Method for recycling of phenolic antioxidant agent, process for production of olefin polymer, polyolefin powder, and fibers

ABSTRACT

Provided are a recycling method for industrially, simply and effectively recycling a phenolic body from a phenolic antioxidant which is masked by an organoaluminum compound and contained in an olefin polymer obtained by supplying the masked phenolic antioxidant upon polymerization; and an olefin polymer obtained by this method. 
     In a method for recycling a phenolic antioxidant wherein a phenolic antioxidant which is masked by an organoaluminum compound and contained in an olefin polymer obtained by supplying the masked phenolic antioxidant upon polymerization is recycled to a phenolic body, a nitrogen gas comprising water and/or a proton donor at a volume ratio of 1.0×10 −6  to 2.5×10 −2  with respect to 1 volume of nitrogen is brought into contact with the olefin polymer.

This application is a Divisional of application Ser. No. 13/391,078,filed Mar. 1, 2012, which is the National Stage of InternationalApplication No. PCT/JP2010/064954, filed Sep. 1, 2010, and which claimspriority to Japanese Application No. 2009-204699, filed Sep. 4, 2009,Japanese Application No. 2009-204700, filed Sep. 4, 2009, JapaneseApplication No. 2009-204701, filed Sep. 4, 2009 and Japanese ApplicationNo. 2009-228981, filed Sep. 30, 2009, and all the benefits accruingtherefrom under 35 U.S.C. 119, the content of which is incorporatedherein by reference in its entirety.

TECHNICAL FIELD

The present invention relates to a method for recycling a phenolicantioxidant used for stabilization of macromolecular materials, and anolefin polymer, more particularly, a method for industrially, simply andeffectively recycling a phenolic body from a phenolic antioxidant whichis masked by an organoaluminum compound and contained in an olefinpolymer obtained by supplying the masked phenolic antioxidant uponpolymerization; and an olefin polymer obtained by this method.

Further, the present invention relates to a method for producing anolefin polymer, more particularly, a method for producing a stabilizedolefin polymer, wherein a phenolic antioxidant masked by anorganoaluminum compound is supplied upon polymerization when olefinmonomers are polymerized, which method enables to industrially, simplyand effectively recycle the phenolic antioxidant which is masked by theorganoaluminum and contained in the olefin polymer to a phenolic body.

Further, the present invention relates to a method for producing astabilized olefin polymer, more particularly, a method for producing astabilized olefin polymer wherein fluidity of an additive is improved,the concentration of a slurry additive is less likely to become unevenwith time, and the quality of the polymer is constant.

Still further, the present invention relates to a polyolefin powder anda fiber obtained using it, more particularly, a polyolefin powder withwhich a polyolefin fiber having good thermal stability and excellent NOxgas resistance can be provided, and a fiber obtained using it.

BACKGROUND ART

As a method wherein a stabilizer is added before polymerization orduring polymerization of olefins, Patent Document 1 proposes a methodwherein olefin monomers are polymerized in the presence of a phenolicantioxidant. A method wherein a phenolic antioxidant is added before thepolymerization or during the polymerization has the advantage of beingable to omit a step of blending of the stabilizer by melt-kneading suchas extruding after the polymerization, but it has been suggested thatphenolic antioxidants having an ester bond such astetrakis(3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionyloxymethyl)methanehave problems in that the catalytic activity of a polymerizationcatalyst may decreased; the interaction between a stabilizer and a metalin a polymerization catalyst may cause coloring of olefins; and thelike, so that selection and control of polymerization conditions arelaborious, which is problematic.

The present inventors reported in Patent Document 2, Patent Document 3and Patent Document 4 that masking of a specific phenolic antioxidant byan organoaluminum compound can solve the above-described problems.However, although a phenolic antioxidant masked by an organoaluminumcompound suppresses adverse effects on a polymerization catalyst, theeffect of the action of the phenolic antioxidant as a stabilizer cannotbe obtained in cases where the masked phenolic antioxidant is used as itis, so that a step of recycling of the masked phenolic antioxidant to aphenolic body is required after polymerization of olefin monomers.

In Patent Documents 2 to 4, methods wherein a phenolic antioxidant isrecycled by an alcohol, water or water vapor employed in a step ofremoval of the polymerization catalyst residue after completion of apolymerization step are proposed. Actually, by sufficiently carrying outthe polymerization catalyst deactivation treatment after completion ofbatch polymerization with an alcohol, water or water vapor, a maskedphenolic antioxidant can be recycled to a phenolic body and a sufficientstabilization effect can therefore be achieved.

Further, a method for producing a fiber by the melt-blown method using apolyester polymer is known. The melt-blown method is a method wherein amolten resin is extruded to form a small resin flow, which is thenbrought into contact with a high-speed heated gas to be made into adiscontinuous fiber having a small fiber diameter, followed byaccumulating this fiber on a porous support, to obtain a fiber. By usingthe melt-blown method, productivity of polyester resin fibers has beenimproved. Use of the melt-blown method is being studied also for othervarious materials, and its use has been attempted also for polyolefins.

Polyolefins have a problem in that they have poor stability to heat andlight and hence are easily oxidized/deteriorated when the polyolefinsare processed at a high temperature and when they are exposed to heatand/or light during their use, resulting in insufficient service livesas plastic products. Thus, in general, in order to preventoxidation/deterioration, a stabilizer(s) such as a phenolic antioxidant,phosphorus-containing antioxidant, sulfur-containing antioxidant,hydroxylamine compound, hindered amine compound, ultraviolet absorberand/or acid scavenger is/are added. Selection, blending and the like ofvarious stabilizers depending on the intended use are being studied torealize their practical uses.

In cases where a stabilizer is blended in a polyolefin, a method whereinthe polyolefin and the stabilizer are mixed together and granulation isthen carried out using an extrusion apparatus or the like is generallyemployed, and, for example, Patent Document 5 and Patent Document 6propose polyolefin resin compositions prepared by inclusion of a1,3,5-tris-(4-t-butyl-3-hydroxy-2,6-dimethylbenzyl)isocyanurate phenolicantioxidant and a phosphorus-containing antioxidant in a polyolefinresin.

However, in cases where a fiber is to be obtained by the melt-blownmethod, there is a problem in that, since the polyolefin employed hasextremely high fluidity (in some cases, a melt flow rate of 200 to 600g/10 min.), granulation is impossible with a usual extrusion apparatus.

As a method for stabilizing a polyolefin wherein a granulation stepusing an extrusion apparatus is not employed, methods wherein astabilizer is added before polymerization or after polymerization ofolefin monomers have been studied. For example, in Patent Document 7, aproduction method wherein α-olefins are polymerized in the presence of aphosphorus-containing antioxidant is shown. It is shown that, whencompared to polyolefins produced by mixing an antioxidant with a polymerobtained by polymerization of α-olefins without using aphosphorus-containing antioxidant, polyolefins produced by polymerizingα-olefins in the presence of a phosphorus-containing antioxidant havemore excellent stabilization effects.

Although a method wherein a stabilizer is added before polymerization orafter polymerization of olefin monomers has the advantage of being ableto omit a step of blending of the stabilizer by melt-kneading such asextruding after the polymerization, the method has problems in that thecatalytic activity of a polymerization catalyst may be decreased; theinteraction between a stabilizer and a catalyst metal may cause coloringof the polyolefin resin; and the like, so that selection and control ofpolymerization conditions are laborious, which is problematic.

Examples of particular influences of the stabilizer on thepolymerization catalyst include, as suggested in Patent Document 1,lowering of the catalytic activities of polymerization catalysts byphenolic antioxidants having an ester bond, such astetrakis[3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionyloxymethyl]methane,which are stabilizers widely used for polyolefins. Thus, it has beenshown that such phenolic antioxidants are not suitable for being addedbefore the polymerization.

As methods for avoiding such influences on polymerization catalysts,Patent Document 3 and Patent Document 4 describe methods wherein aphenolic antioxidant masked by an organoaluminum compound is addedbefore polymerization or during polymerization of monomers having anethylenically unsaturated bond, to produce a stabilized polymer.

RELATED ART DOCUMENTS Patent Documents

-   Patent Document 1: Japanese Unexamined Patent Application    Publication No. 5-271335-   Patent Document 2: Japanese Unexamined Patent Application    Publication No. 2005-255953-   Patent Document 3: Japanese Unexamined Patent Application    Publication No. 2006-052241-   Patent Document 4: Japanese Unexamined Patent Application    Publication No. 2006-282985-   Patent Document 5: Japanese Unexamined Patent Application    Publication No. 10-183423-   Patent Document 6: Japanese Unexamined Patent Application    Publication No. 57-3842-   Patent Document 7: Japanese Unexamined Patent Application    Publication No. 63-92613

SUMMARY OF THE INVENTION Problems to be Solved by the Invention

In cases where the stabilization methods of the above Patent Documentsare to be applied to gas-phase polymerization or bulk polymerization, aphenolic antioxidant masked by an organoaluminum is preliminarilyprepared and added to a catalyst, followed by supplying the resultingmixture to a polymerization apparatus. Since, as a result, a step ofhandling of an organoaluminum compound, whose contacting with oxygen ormoisture should be avoided, is added to a conventional polymerizationmethod, the operation is laborious, and safety of the operation andmaintenance of stability of the polymerization activity must be takeninto consideration, which prevent the methods from being industriallyused.

Further, although a phenolic antioxidant itself has poor fluidity andhence needs to be slurried with a solvent, diffusibility of a phenolicantioxidant in a solution is poor and therefore the phenolic antioxidantprecipitates with time to cause unevenness of its concentration.Therefore, the stabilization effect of an olefin polymer polymerized bybatch polymerization is not constant, which is problematic.

On the other hand, since, in the cases of continuous polymerization, thelength of time for deactivation of the polymerization catalyst isshorter than in the cases of batch polymerization, the phenolicantioxidant cannot be sufficiently recycled and hence a sufficientstabilization effect cannot be obtained. Further, although a methodwherein the polymerization catalyst is decomposed in a water treatmentstep is preferred in view of securing recycling of the phenolicantioxidant if the water treatment is extensively carried out, increasein the amount of water for the treatment leads to increase in the watercontent of the olefin polymer, and molding of an olefin polymer having ahigh water content may cause problems such as decrease in transparencyof the molded product and generation of air bubbles in the moldedproduct. Further, a larger-scale water treatment step leads to increasein the energy required for separation of the olefin polymer from waterand for a drying step, which is industrially disadvantageous.

In addition, by virtue of the recent progress of catalytic technologiesand polymerization process technologies, the steps of catalystdeactivation and removal of catalyst residues have been largelysimplified, and hence a process requiring no tank for treatment ofcatalyst deactivation and removal of the catalyst residues is becomingcommon. Thus, development of a method by which a phenolic antioxidantcan be effectively recycled while equipment investment for anotherprocess and increase in the processing time can be avoided has beennecessary.

Although the above Patent Documents describe Examples of batch methodsin a laboratory scale, no method for solving the above-describedproblems is described therein, and these literatures do not evendisclose the existence of the above-described problems.

Further, none of the above-described literatures studied application ofthe methods to fibers. Further, during heating (hot air) treatment inthe production process of a polyolefin fiber, the fiber is sometimesexposed to hot air containing a NOx gas, and in this case, the fiberturns yellow due to the influence of the NOx gas and the outerappearance of the polyolefin fiber is degraded, which is problematic.

Thus, the present invention aims to provide a recycling method forindustrially, simply and effectively recycling a phenolic body from aphenolic antioxidant which is masked by an organoaluminum compound andcontained in an olefin polymer obtained by supplying the masked phenolicantioxidant upon polymerization; and an olefin polymer obtained by thismethod.

Another object of the present invention is to provide a method forproducing a stabilized olefin polymer, wherein a phenolic antioxidantmasked by an organoaluminum compound is supplied upon polymerizationwhen olefin monomers are polymerized, which method enables toindustrially, simply and effectively recycle the phenolic antioxidantwhich is masked by the organoaluminum and contained in the olefinpolymer to a phenolic body.

Still another object of the present invention is to provide a method forproducing a stabilized olefin polymer having a constant quality, whereinthe problem of poor fluidity and precipitation of an additive is avoidedand hence the heterogeneity of the concentration of the additive whichoccurs with time is small.

Still another object of the present invention is to provide a polyolefinpowder with which a sufficiently stabilized polyolefin fiber can beprovided while the influence of a NOx gas during the production processis suppressed, and a polyolefin fiber produced using the polyolefinpowder.

Means for Solving the Problems

The present inventors intensively studied to solve the above problemsand discovered that bringing an olefin polymer obtained by supplyingupon polymerization a phenolic antioxidant masked by an organoaluminumcompound into contact with a nitrogen gas containing water and/or aproton donor at a specific ratio enables effective recycling of thephenolic antioxidant masked by an organoaluminum compound and containedin the olefin polymer into a phenolic body.

Further, the present inventors discovered that, when olefin monomers arepolymerized by supplying a phenolic antioxidant masked by anorganoaluminum compound, the above problems can be solved by applyingsteam, or a nitrogen gas containing moisture to the olefin polymer.

Further, the present inventors discovered that the above problems can besolved by inclusion, upon polymerization of olefin monomers, of a stepwherein a slurry additive(s) is/are pumped while being mixed with apromoter component(s) in a pipe(s), followed by transferring theresulting mixture to a polymerization tank.

Still further, the present inventors discovered that the above objectscan be achieved by polymerizing olefin monomers with addition of aspecific phenolic antioxidant masked by an organoaluminum compound, anda phosphorus-containing antioxidant before the polymerization or duringthe polymerization of olefin monomers, thereby completing the presentinvention.

That is, the method of the present invention is a method for recycling aphenolic antioxidant, wherein a phenolic antioxidant represented by theGeneral Formula (1) below:

(wherein R represents C₁₂-C₂₄ alkyl which is optionally branched, C₃-C₁₂cycloalkyl which is optionally substituted, or C₆-C₁₈ aryl whichoptionally has a substituent(s)) which is masked by an organoaluminumcompound and contained in an olefin polymer obtained by supplying themasked phenolic antioxidant upon polymerization is recycled to aphenolic body, wherein

a nitrogen gas comprising water and/or a proton donor at a volume ratioof 1.0×10⁻⁶ to 2.5×10⁻² with respect to 1 volume of nitrogen is broughtinto contact with the olefin polymer.

Further, the method of the present invention is a method for producingan olefin polymer, wherein a phenolic antioxidant represented by theGeneral Formula (1) below:

(wherein R represents C₁₂-C₂₄ alkyl which is optionally branched, C₃-C₁₂cycloalkyl which is optionally substituted, or C₆-C₁₈ aryl whichoptionally has a substituent(s)) which is masked by an organoaluminumcompound is supplied upon polymerization when olefin monomers arepolymerized, wherein

steam, or a nitrogen gas comprising moisture is injected into anextruder when the obtained olefin polymer is melt-kneaded in theextruder.

Further, the method of the present invention is a method for producing astabilized olefin polymer, wherein an additive(s) and a promotercomponent(s) are supplied to olefin monomers upon polymerization of theolefin monomers, wherein

the method comprises a step wherein a slurry additive(s) is/are pumpedwhile being mixed with a promoter component(s) in a pipe(s), followed bytransferring the resulting mixture to a polymerization tank for olefinmonomers.

Further, the polyolefin powder of the present invention is a polyolefinpowder composed of a polyolefin resin composition obtained bypolymerizing olefin monomers, which polyolefin powder is produced byadding 0.001 to 0.5 part by mass of a phenolic antioxidant representedby the General Formula (2) below:

(wherein R represents C₁-C₃₀ alkyl which is optionally branched, C₃-C₁₂cycloalkyl which is optionally substituted, or C₆-C₁₈ aryl whichoptionally has a substituent(s)) masked by an organoaluminum compoundand 0.001 to 0.5 part by mass of a phosphorus-containing antioxidantwith respect to 100 parts by mass of olefin monomers to a catalyticsystem or a polymerization system before polymerization or duringpolymerization of the olefin monomers.

Further, the fiber of the present invention is a fiber obtained by usingthe above-described polyolefin powder.

Effect of the Invention

By the present invention, a phenolic body can be industrially, simplyand effectively recycled from a phenolic antioxidant which is masked byan organoaluminum compound and contained in an olefin polymer obtainedby supplying the masked phenolic antioxidant upon polymerization.

Further, by the present invention, when olefin monomers are polymerizedby supplying upon polymerization a phenolic antioxidant masked by anorganoaluminum compound, the phenolic antioxidant which is masked by anorganoaluminum compound and contained in the olefin polymer can beindustrially, simply and effectively recycled into a phenolic body, anda stabilized olefin polymer can be produced.

Further, by the present invention, a method for producing a stabilizedolefin polymer having a constant quality, wherein the problem of poorfluidity and precipitation of an additive is avoided and hence theheterogeneity of the concentration of the additive which occurs withtime is small, can be provided.

Further, by the present invention, a polyolefin powder with which asufficiently stabilized polyolefin fiber can be provided while theinfluence of a NOx gas during the production process is suppressed, anda polyolefin fiber produced using the polyolefin powder can be provided.

BEST MODE FOR CARRYING OUT THE INVENTION

The modes of the present invention will now be described moreparticularly.

The phenolic antioxidant to be used in the present invention is notrestricted as long as the phenolic antioxidant is not decomposed bymasking treatment with an organoaluminum compound, and examples of thephenolic antioxidant include amide compounds of3-(3,5-dialkyl-4-hydroxyphenyl)propionate such asstearyl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide,palmityl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide,myristyl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide andlauryl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide; and1,3,5-trimethyl-2,4,6-tris(3,5-di-tert-butyl-4-hydroxybenzyl)benzene.

Among the above phenolic antioxidants, compounds represented by theGeneral Formula (1) below:

(wherein R represents C₁-C₃₀ alkyl which is optionally branched, C₃-C₁₂cycloalkyl which is optionally substituted, or C₆-C₁₈ aryl whichoptionally has a substituent(s)), such asstearyl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide,palmityl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide,myristyl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide andlauryl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide, are especiallypreferred since these are excellent in the effect of stabilization ofolefin polymers and color tone.

Examples of the C₁-C₃₀ alkyl which is optionally branched, representedby R in the General Formula (1), include methyl, ethyl, propyl,isopropyl, butyl, sec-butyl, tert-butyl, isobutyl, pentyl, isopentyl,tert-pentyl, hexyl, heptyl, n-octyl, isooctyl, tert-octyl, nonyl,isononyl, decyl, undecyl, dodecyl, tridecyl, tetradecyl, pentadecyl,hexadecyl, heptadecyl and octadecyl, and, in the present invention,those having a number of carbon atoms of 12 to 24 are especiallypreferred. A phenolic antioxidant whose alkyl has less than 12 carbonatoms may be likely to evaporate, while in cases where the alkyl hasmore than 24 carbon atoms, the ratio of phenol with respect to themolecular weight of the phenolic antioxidant is small and hence thestabilization effect may be decreased.

These alkyl groups may be interrupted by an oxygen atom(s) and/or sulfuratom(s), and/or an aryl group(s) described below, and/or a hydrogenatom(s) in the alkyl groups may be substituted by a chain aliphaticgroup(s) such as hydroxy, cyano, alkenyl and/or alkenyloxy; a cyclicaliphatic group(s) such as pyrrole, furan, thiophene, imidazole,oxazole, thiazole, pyrazole, isoxazole, isothiazole, pyridine,pyridazine, pyrimidine, pyrazine, piperidine, piperazine, morpholine,2H-pyran, 4H-pyran, phenyl, biphenyl, triphenyl, naphthalene,anthracene, pyrrolidine, pyrindine, indolizine, indole, isoindole,indazole, purine, quinolizine, quinoline, isoquinoline and/orcycloalkyl; and/or an aromatic group(s). Further, two or more of theseinterruptions and/or substitutions may be combined.

Examples of the C₃-C₁₂ cycloalkyl which is optionally substituted,represented by R in the General Formula (1), include cyclopropyl,cyclopentyl, cyclohexyl, cycloheptyl, cyclooctyl, cyclononyl andcyclodecyl, and a hydrogen atom(s) in the cycloalkyl may be substitutedby alkyl, alkenyl, alkenyloxy, hydroxy and/or cyano, which alkyl may beinterrupted by an oxygen atom(s) and/or a sulfur atom(s).

Examples of the C₆-C₁₈ aryl which optionally has a substituent(s),represented by R in the General Formula (1), include phenyl,methylphenyl, butylphenyl, octylphenyl, 4-hydroxyphenyl,3,4,5-trimethoxyphenyl, 4-tert-butylphenyl, biphenyl, naphthyl,methylnaphthyl, anthracenyl, phenanthryl, benzyl, phenylethyl and1-phenyl-1-methylethyl. Further, a hydrogen atom(s) in the aryl may besubstituted by alkyl, alkenyl, alkenyloxy, hydroxy and/or cyano, whichalkyl may be interrupted by an oxygen atom(s) or sulfur atom(s).

Particular Examples of the structure of the phenolic antioxidantrepresented by General Formula (1) include the Compounds No. 1 to No. 16described below. However, the present invention is not restricted by thecompounds below.

The phenolic antioxidant is used preferably in an amount of 0.001 to 0.5part by mass, more preferably in an amount of 0.005 to 0.3 part by masswith respect to 100 parts by mass of olefin monomers.

The additive(s) used in the method for producing a stabilized olefinpolymer, wherein an additive(s) and a promoter component(s) are suppliedto olefin monomers upon polymerization of the olefin monomers,characterized in that the method comprises a step wherein a slurryadditive(s) is/are pumped while being mixed with a promoter component(s)in a pipe(s), followed by transferring the resulting mixture to apolymerization tank for olefin monomers, is/are not restricted as longas the additive(s) can be added to olefin polymers, and the additive(s)preferably contain(s) a phenolic antioxidant. The phenolic antioxidantis not restricted as long as the phenolic antioxidants is not decomposedby masking treatment with an organoaluminum compound, and examples ofthe phenolic antioxidant to be employed include amide compounds of3-(3,5-dialkyl-4-hydroxyphenyl)propionate such asstearyl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide,palmityl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide,myristyl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide andlauryl-3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionamide; and1,3,5-trimethyl-2,4,6-tris(3,5-di-tert-butyl-4-hydroxybenzyl)benzene.The phenolic antioxidant is especially preferably one represented byGeneral Formula (1):

(wherein R represents C₁-C₃₀ alkyl which is optionally branched, C₃-C₁₂cycloalkyl which is optionally substituted, or C₆-C₁₈ aryl whichoptionally has a substituent(s)).

The substituent(s), amount used, and particular examples of the phenolicantioxidant represented by the General Formula (1) are the same as thosedescribed above.

The phenolic antioxidant used in the polyolefin powder of the presentinvention is a compound represented by the General Formula (2) below:

(wherein R represents C₁-C₃₀, preferably C₁₂-C₂₄ alkyl which isoptionally branched, C₃-C₁₂ cycloalkyl which is optionally substituted,or C₆-C₁₈ aryl which optionally has a substituent(s)),and used preferably in an amount of 0.001 to 0.5 part by mass, morepreferably in an amount of 0.005 to 0.3 part by mass with respect to 100parts by mass of olefin monomers.

Examples of the C₁-C₃₀ alkyl which is optionally branched, representedby R in the General Formula (2), include methyl, ethyl, propyl,isopropyl, butyl, sec-butyl, tert-butyl, pentyl, sec-pentyl,tert-pentyl, dodecyl, tridecyl, tetradecyl, pentadecyl, hexadecyl,heptadecyl, octadecyl and 1,5-dimethyl-hexyl.

These alkyl groups may be interrupted by an oxygen atom(s) or sulfuratom(s), or an aryl group(s) described below, and a hydrogen atom(s) inthe alkyl groups may be substituted by a chain aliphatic group(s) suchas hydroxy, cyano, alkenyl and/or alkenyloxy; a cyclic aliphaticgroup(s) such as pyrrole, furan, thiophene, imidazole, oxazole,thiazole, pyrazole, isoxazole, isothiazole, pyridine, pyridazine,pyrimidine, pyrazine, piperidine, piperazine, morpholine, 2H-pyran,4H-pyran, phenyl, biphenyl, triphenyl, naphthalene, anthracene,pyrrolidine, pyrindine, indolizine, indole, isoindole, indazole, purine,quinolizine, quinoline, isoquinoline and/or cycloalkyl; and/or anaromatic group(s). Further, a combination of two or more of theseinterruptions and/or substitutions may be combined.

Examples of the C₃-C₁₂ cycloalkyl which is optionally substituted,represented by R in the General Formula (2), include cyclopropyl,cyclopentyl, cyclohexyl, cycloheptyl, cyclooctyl, cyclononyl andcyclodecyl, and a hydrogen atom(s) in the cycloalkyl may be substitutedby alkyl, alkenyl, alkenyloxy, hydroxy and/or cyano, which alkyl may beinterrupted by an oxygen atom(s) and/or a sulfur atom(s).

Examples of the C₆-C₁₈ aryl which optionally has a substituent(s),represented by R in the General Formula (2), include phenyl,methylphenyl, butylphenyl, octylphenyl, 4-hydroxyphenyl,3,4,5-trimethoxyphenyl, 4-tert-butylphenyl, biphenyl, naphthyl,methylnaphthyl, anthracenyl, phenanthryl, benzyl, phenylethyl and1-phenyl-1-methylethyl. Further, a hydrogen atom(s) in the aryl may besubstituted by alkyl, alkenyl, alkenyloxy, hydroxy and/or cyano, whichalkyl may be interrupted by an oxygen atom(s) or sulfur atom(s).

Particular examples of the structure of the phenolic antioxidantrepresented by General Formula (2) include the Compounds No. 1 to No. 16described above. However, the present invention is not restricted by thecompounds described above.

Examples of the organoaluminum compound which may be used for maskingthe phenolic antioxidant include alkylaluminums and alkylaluminumhydrides, among which alkylaluminums are preferred, and trialkylaluminums are especially preferred. Particular examples of the trialkylaluminums include trimethyl aluminum, triethyl aluminum, tri-n-propylaluminum, triisobutyl aluminum, tri-n-hexyl aluminum and tri-n-octylaluminum. A mixture of any of the above organoaluminum compounds may beused. Aluminoxane, which is obtained by reaction of an alkylaluminum oran alkylaluminum hydride with water, may be similarly used.

The phenolic antioxidant masked by an organoaluminum compound means aphenolic antioxidant wherein the hydrogen atom of its phenolic hydroxylgroup is substituted by an organoaluminum compound, which maskedphenolic antioxidant can be recycled into a phenolic body by treatmentwith a hydrogen donor compound such as water, an alcohol or an acid.Among these, those which can recycle phenol by reacting with aninactivator used for deactivation treatment of a catalyst in thepolymerization reaction are preferred, and a phenolate (salt) obtainedby reaction of an organoaluminum compound with a phenolic antioxidant isespecially preferred, which organoaluminum compound normally exists inthe polymerization system by a polymerization catalyst for an olefinresin and does not inhibit the polymerization.

The method of the above-described masking can be simply carried out bymixing the organoaluminum compound with the phenolic antioxidant in aninert solvent and stirring the resulting mixture. In the reaction bythis method, in cases where a by-produced compound does not affect thepolymerization product, the phenolic antioxidant can be used as it is,but in cases where a by-produced compound inhibits the polymerization,the by-produced compound is preferably removed by evaporation underreduced pressure or the like before use of the phenolic antioxidant.

Examples of the inert solvent include aliphatic and aromatic hydrocarboncompounds. Examples of the aliphatic hydrocarbon compounds includesaturated hydrocarbon compounds such as n-pentane, n-hexane, n-heptane,n-octane, isooctane and purified kerosene; and cyclic saturatedhydrocarbon compounds such as cyclopentane, cyclohexane andcycloheptane; and examples of the aromatic hydrocarbon compounds includecompounds such as benzene, toluene, ethylbenzene and xylene. Among thesecompounds, n-hexane or n-heptane is preferably used. The concentrationof the trialkyl aluminum salt in the inert solvent is preferably withinthe range of 0.001 to 0.5 mol/L, especially preferably within the rangeof 0.01 to 0.1 mol/L.

Examples of the olefin monomers to obtain the olefin polymer used in thepresent invention include ethylene, propylene, 1-butene, 1-hexene,3-methyl-1-butene, 3-methyl-1-pentene, 4-methyl-1-pentene,vinylcycloalkane and styrene, and derivatives thereof.

The olefin polymer is obtained by homopolymerization of the olefinmonomers or by copolymerization in which the olefin monomers areinvolved, and examples of the olefin polymer include polypropylenes suchas propylene homopolymers, ethylene-propylene copolymers, and copolymersof propylene and an α-olefin(s) other than propylene, includingethylene-propylene-butene copolymers; polyethylenes such as high-densitypolyethylenes, linear low-density polyethylenes and low-densitypolyethylenes; and cycloolefins.

The polymerization of olefin monomers needs to be carried out in thepresence of a polymerization catalyst under an atmosphere of an inertgas such as nitrogen, or the polymerization may be carried out in theinert solvent described above. Further, as long as the polymerization isnot inhibited, an active hydrogen compound, fine particle carrier,organoaluminum compound, ion-exchangeable layered compound and/orinorganic silicate may be added.

In the present invention, the polymerization catalyst is not restricted,and a known polymerization catalyst may be used. Examples of thepolymerization catalyst include compounds of the transition metalsbelonging to the groups 3 to 11 in the periodic table (e.g., titanium,zirconium, hafnium, vanadium, iron, nickel, lead, platinum, yttrium andsamarium), and representative examples of the polymerization catalystwhich may be used include Ziegler catalysts, Ziegler-Natta catalystscomposed of a titanium-containing solid transition metal component andan organic metal component, metallocene catalysts composed of a compoundof a transition metal belonging to the group 4 to 6 in the periodictable having at least one cyclopentadienyl skeleton and a promotercomponent, and chrome catalysts.

Examples of the method of polymerization of olefin monomers includemethods wherein olefin monomers are polymerized to produce an olefinhomopolymer and methods wherein propylene and at least one type ofolefin (excluding propylene) unit selected from the group consisting ofolefin units having 2 to 12 carbon atoms are copolymerized to produce acopolymer, which methods are carried out by slurry polymerization,wherein polymerization is carried out in an inert solvent such as analiphatic hydrocarbon including butane, pentane, hexane, heptane orisooctane, alicyclic hydrocarbon including cyclopentane, cyclohexane ormethylcyclohexane; aromatic hydrocarbon such as toluene, xylene orethylbenzene; gasoline fraction; or hydrogenated diesel fraction;gas-phase polymerization, wherein polymerization is carried out in a gasphase; bulk polymerization, wherein the olefin monomers themselves areused as a solvent; solution polymerization, wherein a polymer isproduced in the form of a liquid; a polymerization method by acombination of two or more of these methods; single-stagepolymerization; or multistage polymerization. Further, either abatch-type or continuous-type production method can be used.

In the present invention, in polymerization equipment for bulkpolymerization or gas-phase polymerization, or for the combination ofthese methods, the present invention can be applied using the existingpolymerization equipment without modification of the equipment, so thatsuch polymerization equipment is preferably used, and one used for thecontinuous method is industrially advantageous and hence preferred. Inthe case of batch polymerization, a masked phenolic antioxidantsometimes precipitates with time and is solidified in a tank. Further,although the present invention can be used also in slurrypolymerization, solution polymerization and the like, thesepolymerization methods require a step of drying olefin polymers,resulting in increase in the energy of production, so that these methodsare not preferred in view of power saving.

As a polymerization tank used in the above-described polymerizationmethods, a continuous reactor in existing equipment may be used withoutmodification, and the present invention is not restricted by the size,shape, material and the like of the conventional polymerizationequipment.

In the method of the present invention for recycling a phenolicantioxidant which is masked by an organoaluminum compound and containedin an olefin polymer obtained as mentioned above, a nitrogen gascomprising water and/or a proton donor at a volume ratio of 1.0×10⁻⁶ to2.5×10⁻², preferably 1.0×10⁻³ to 1.5×10⁻² with respect to 1 volume ofnitrogen is brought into contact with the olefin polymer. In cases wherethe volume ratio with respect to 1 volume of nitrogen is less than1.0×10⁻⁶, recycling of the masked phenolic antioxidant takes a longtime, while in cases where the volume ratio is more than 2.5×10⁻², thewater content of the obtained olefin polymer is high and bubbles may begenerated during processing. For application of the present invention toa continuous production method, the equipment may be one wherein, in atank to which an olefin polymer is intermittently or continuouslysupplied, the above-described nitrogen gas can be brought into contactwith the olefin polymer. For example, the equipment may be one wherein,in a cylindrical column, an olefin polymer is intermittently orcontinuously supplied from the upper side of the column and the nitrogengas is supplied from the bottom of the column, or one wherein an olefinpolymer is supplied from the upper side of a tank and the nitrogen gasis supplied from the lower side, which column or tank can discharge theolefin polymer containing a phenolic antioxidant recycled into aphenolic body. Particular examples of the tank include purge columns andsteamers.

The proton donor means an active substance which substitutes a hydroxylgroup, and examples thereof include alcohols such as methanol, ethanol,1-propanol, 2-propanol, n-butanol, isobutanol, sec-butanol,tert-butanol, ethylene glycol and glycerin; phenolic substances; andmineral acids such as hydrochloric acid and sulfuric acid. In thepresent invention, methanol or ethanol is preferably used.

In the method for producing an olefin polymer, wherein a phenolicantioxidant represented by the General Formula (1) which is masked by anorganoaluminum compound is supplied upon polymerization when olefinmonomers are polymerized, characterized in that steam, or a nitrogen gascomprising moisture is injected into an extruder when the obtainedolefin polymer is melt-kneaded in the extruder, it is possible, bybringing steam, or the gas comprising moisture into contact with theolefin polymer when the olefin polymer is melt-kneaded, to recycle thephenolic antioxidant which is masked by an organoaluminum compound andcontained in the olefin polymer into a phenolic body. It is especiallypreferred to install an extruder for mixing as required the olefinpolymer with another additive and melt-kneading the resulting mixture,and to introduce steam into the extruder, since further equipmentinvestment is unnecessary in such a case.

The above extruder can be used irrespective of which extrusion method,among the methods such as the uniaxial, biaxial and multiaxial method,is employed, and is not restricted as long as an olefin polymer can bemelt and kneaded therewith and steam can be introduced thereto.

In the method for producing a stabilized olefin polymer, wherein anadditive(s) and a promoter component(s) are supplied to olefin monomersupon polymerization of the olefin monomers, characterized in that themethod comprises a step wherein a slurry additive(s) is/are pumped whilebeing mixed with a promoter component(s) in a pipe(s), followed bytransferring the resulting mixture to a polymerization tank for olefinmonomers, each additive needs to be in the form of a slurry in order tobe supplied to the pipe(s) through which the promoter(s) is/aretransferred from a supplying tank(s) of the promoter(s) to apolymerization tank. In cases where each additive is in the form of aliquid, the additive can be transferred as it is, while in cases wherethe additive is solid, the additive may be, for example, supplied afterbeing mixed with a solvent to be made into a suspended state(slurrying). Further, in cases where the additive is solid, theconcentration of the additive in the slurry is preferably within therange of 1 to 80% by mass, and the additive is preferably in a fluidstate.

Examples of the above solvent include aliphatic hydrocarbons andalicyclic hydrocarbons. Examples of the aliphatic hydrocarbons includesaturated hydrocarbon compounds such as n-pentane, n-hexane, n-heptane,n-octane, isooctane and purified kerosene; and examples of the alicyclichydrocarbons include cyclopentane, cyclohexane and cycloheptane. In thepresent invention, n-hexane, n-heptane or paraffin is preferably used.The concentration of the promoter in the solvent is preferably withinthe range of 0.001 to 0.5 mol/L, especially preferably 0.01 to 0.1mol/L.

The olefin monomers are not restricted, and examples thereof include theabove-described monomers.

Polymerization of the olefin monomers may be carried out in the samemanner as described above.

The polymerization catalyst is not restricted, and those which are thesame as described above may be used.

Examples of the method of polymerization of the olefin monomers includethose which are the same as described above.

Examples of the polymerization tank which may be used include thosewhich are the same as described above.

The olefin polymer is obtained by homopolymerization of the above olefinmonomers or by copolymerization in which olefin monomers are involved,and examples of the olefin polymer include polypropylenes such aspropylene homopolymers, ethylene-propylene copolymers, and copolymers ofpropylene and an α-olefin(s) other than propylene, includingethylene-propylene-butene copolymers; polyethylenes such as high-densitypolyethylenes, linear low-density polyethylenes and low-densitypolyethylenes; and cycloolefin polymers.

In the polyolefin powder of the present invention, the phenolicantioxidant masked by an organoaluminum means a phenolic antioxidantwherein the hydrogen atom of its phenolic hydroxyl group is substitutedby an organoaluminum compound, which phenolic antioxidant was masked bytreatment with a hydrogen donor compound such as water, an alcohol or anacid such that the phenolic antioxidant can be recycled into phenol.Among these, those which can recycle phenol by reacting with aninactivator used for deactivation treatment of a catalyst in thepolymerization reaction are preferred, and a phenolate (salt) obtainedby reaction of an organoaluminum compound with a phenolic antioxidant isespecially preferred, which organoaluminum compound normally exists in apolymerization system by a polymerization catalyst for a polyolefinresin and does not inhibit the polymerization.

Examples of the organoaluminum compound include those which are the sameas described above.

The masking of a phenolic antioxidant can be simply carried out bymixing a metal compound such as a trialkyl aluminum with a phenolicantioxidant in an inert solvent and stirring the resulting mixture. Inthe reaction by this method, in cases where a by-produced compound doesnot affect the polymerization product, the phenolic antioxidant can beused as it is, but in cases where a by-produced compound inhibits thepolymerization, the by-produced compound is preferably removed byevaporation under reduced pressure or the like before use of thephenolic antioxidant.

Examples of the inert solvent include those which are the same asdescribed above.

Examples of the phosphorus-containing antioxidant include triphenylphosphite, trisnonylphenyl phosphite,tris(2,4-di-tert-butylphenyl)phosphite,tris(2,4-di-tert-butyl-5-methylphenyl)phosphite, tris[2-tert-butyl4-(3-tert-butyl-4-hydroxy-5-methylphenylthio)-5-methylphenyl]phosphite,tridecyl phosphite, octyl diphenyl phosphite, di(decyl)monophenylphosphite, di(tridecyl)pentaerythritol diphosphite,di(nonylphenyl)pentaerythritol diphosphite,bis(2,4-di-tert-butylphenyl)pentaerythritol diphosphite,bis(2,6-di-tert-butyl-4-methylphenyl)pentaerythritol diphosphite,bis(2,4,6-tri-tert-butylphenyl)pentaerythritol diphosphite,bis(2,4-dicumylphenyl)pentaerythritol diphosphite,tetra(tridecyl)isopropylidenediphenol diphosphite,tetra(tridecyl)-4,4′-n-butylidenebis(2-tert-butyl-5-methylphenol)diphosphite,hexa(tridecyl)-1,1,3-tris(2-methyl-4-hydroxy-5-tert-butylphenyl)butanetriphosphite, tetrakis(2,4-di-tert-butylphenyl)biphenylenediphosphonite, 9,10-dihydro-9-oxa-10-phosphaphenanthrene-10-oxide,2,2′-methylenebis(4,6-di-tert-butylphenyl)-2-ethylhexyl phosphite,2,2′-methylenebis(4,6-di-tert-butylphenyl)-octadecyl phosphite,2,2′-ethylidenebis(4,6-di-tert-butylphenyl)fluorophosphite,tris(2-[(2,4,8,10-tetrakis-tert-butyldibenzo[d,f][1,3,2]dioxaphosphepin-6-yl)oxy]ethyl)amine,and known phosphorus-containing antioxidants of2-ethyl-2-butylpropyleneglycol and 2,4,6-tri-tert-butylphenol. Thephosphorus-containing antioxidant is preferably one such astris(2,4-di-tert-butylphenyl)phosphite, which does not adversely affectpolymerization even in cases where the phosphorus-containing antioxidantis added before polymerization of olefin monomers.

The amount of the phosphorus-containing antioxidant used is preferably0.001 to 3 parts by weight, more preferably 0.005 to 0.5 part by weightwith respect to 100 parts by weight of the polyolefin resin.

Examples of the olefin monomers used for the polyolefin powder of thepresent invention include those described above.

Examples of the polymerization catalyst used for the polyolefin powderof the present invention include those described above.

The polymerization of olefin monomers needs to be carried out under anatmosphere of an inert gas such as nitrogen, or the polymerization maybe carried out in the inert solvent described above. Further, as long asthe polymerization is not inhibited, an active hydrogen compound, fineparticle carrier, organoaluminum compound, ion-exchangeable layeredcompound and/or inorganic silicate may be added.

Examples of the method of polymerization of olefin monomers includemethods wherein olefin monomers are polymerized to produce an olefinhomopolymer and methods wherein propylene and at least one type ofolefin (excluding propylene) unit selected from the group consisting ofolefin units having 2 to 12 carbon atoms are copolymerized to produce acopolymer, which methods are carried out by slurry polymerization,gas-phase polymerization, bulk polymerization, solution polymerization,a polymerization method by a combination of two or more of thesemethods, single-stage polymerization, or multistage polymerization.Further, the production can be carried out irrespective of whether themethod is a batch method or a continuous method. Upon completion of thepolymerization, the catalyst can be decomposed by addition of water(vapor) or an alcohol.

To the olefin polymer, another additive which is normally used may beadded as required. In a blending method of the another additive, theadditive may be added upon polymerization as long as the additive doesnot inhibit the polymerization. Further examples of the method include amethod wherein the another additive is mixed with an olefin polymer at ablending ratio which varies depending on the object, and the resultingmixture is then melt-kneaded in a processor such as an extruder to carryout granulation or molding.

In a method for producing an olefin polymer, wherein a phenolicantioxidant represented by the General Formula (1) below which is maskedby an organoaluminum compound is supplied upon polymerization whenolefin monomers are polymerized, characterized in that steam, or anitrogen gas comprising moisture is injected into an extruder when theobtained olefin polymer is melt-kneaded in the extruder, this processingmay be carried out either at the same time as or after the introductionof steam.

Examples of the another additive include phosphorus-containingantioxidants, ultraviolet absorbers, hindered amine compounds, heavymetal deactivators, nucleating agents, flame retardants, metallic soaps,hydrotalcites, fillers, lubricants, antistatic agents, pigments, dyesand plasticizers, or a phenolic antioxidant may be further added as theanother additive.

Further, to the polyolefin powder of the present invention, stillanother additive which is normally used may be blended as required.Examples of the blending method of the another additive include a methodwherein the additive is slurried by being dissolved in a saturatedcarbon solvent to an extent at which polymerization of olefin monomersare not inhibited, and the resulting slurry is then added when olefinmonomers are polymerized. Further, if possible, the another additive maybe mixed at a blending ratio which varies depending on the object, andthe resulting mixture may be then melt-kneaded in a processor such as anextruder to carry out granulation. Examples of the another additiveinclude ultraviolet absorbers, hindered amine compounds, heavy metaldeactivators, nucleating agents, flame retardants, metallic soaps,hydrotalcites, fillers, lubricants, antistatic agents, pigments, dyesand plasticizers, and, a phenolic antioxidant and/orphosphorus-containing antioxidant used in the present invention and/oranother phenolic antioxidant may also be added after the polymerization,followed by processing the resulting polymer.

Examples of the phosphorus-containing antioxidant include thosedescribed above.

The amount of the phosphorus-containing antioxidant to be used ispreferably 0.001 to 3 parts by weight, more preferably 0.005 to 0.5 partby weight with respect to 100 parts by weight of the olefin polymer.

Examples of the ultraviolet absorbers include 2-hydroxybenzophenonessuch as 2,4-dihydroxybenzophenone, 2-hydroxy-4-methoxybenzophenone,2-hydroxy-4-octoxybenzophenone and5,5′-methylenebis(2-hydroxy-4-methoxybenzophenone);2-(2-hydroxyphenyl)benzotriazoles such as2-(2-hydroxy-5-methylphenyl)benzotriazole,2-(2-hydroxy-5-tert-octylphenyl)benzotriazole,2-(2-hydroxy-3,5-di-tert-butylphenyl)-5-chlorobenzotriazole,2-(2-hydroxy-3-tert-butyl-5-methylphenyl)-5-chlorobenzotriazole,2-(2-hydroxy-3,5-dicumylphenyl)benzotriazole,2,2′-methylenebis(4-tert-octyl-6-benzotriazolylphenol), polyethyleneglycol esters of2-(2-hydroxy-3-tert-butyl-5-carboxyphenyl)benzotriazole,2-[2-hydroxy-3-(2-acryloyloxyethyl)-5-methylphenyl]benzotriazole,2-[2-hydroxy-3-(2-methacryloyloxyethyl)-5-tert-butylphenyl]benzotriazole,2-[2-hydroxy-3-(2-methacryloyloxyethyl)-5-tert-octylphenyl]benzotriazole,2-[2-hydroxy-3-(2-methacryloyloxyethyl)-5-tert-butylphenyl]-5-chlorobenzotriazole,2-[2-hydroxy-5-(2-methacryloyloxyethyl)phenyl]benzotriazole,2-[2-hydroxy-3-tert-butyl-5-(2-methacryloyloxyethyl)phenyl]benzotriazole,2-[2-hydroxy-3-tert-amyl-5-(2-methacryloyloxyethyl)phenyl]benzotriazole,2-[2-hydroxy-3-tert-butyl-5-(3-methacryloyloxypropyl)phenyl]-5-chlorobenzotriazole,2-[2-hydroxy-4-(2-methacryloyloxymethyl)phenyl]benzotriazole,2-[2-hydroxy-4-(3-methacryloyloxy-2-hydroxypropyl)phenyl]benzotriazoleand 2-[2-hydroxy-4-(3-methacryloyloxypropyl)phenyl]benzotriazole;2-(2-hydroxyphenyl)-4,6-diaryl-1,3,5-triazines such as2-(2-hydroxy-4-methoxyphenyl)-4,6-diphenyl-1,3,5-triazine,2-(2-hydroxy-4-hexyloxyphenyl)-4,6-diphenyl-1,3,5-triazine,2-(2-hydroxy-4-octoxyphenyl)-4,6-bis(2,4-dimethylphenyl)-1,3,5-triazine,2-[2-hydroxy-4-(3-C₁₂₋₁₃ mixedalkoxy-2-hydroxypropoxy)phenyl]-4,6-bis(2,4-dimethylphenyl)-1,3,5-triazine,2-[2-hydroxy-4-(2-acryloyloxyethoxy)phenyl]-4,6-bis(4-methylphenyl)-1,3,5-triazine,2-(2,4-dihydroxy-3-allylphenyl)-4,6-bis(2,4-dimethylphenyl)-1,3,5-triazineand 2,4,6-tris(2-hydroxy-3-methyl-4-hexyloxyphenyl)-1,3,5-triazine;benzoates such as phenyl salicylate, resorcinol monobenzoate,2,4-di-tert-butylphenyl-3,5-di-tert-butyl-4-hydroxybenzoate,octyl(3,5-di-tert-butyl-4-hydroxy)benzoate,dodecyl(3,5-di-tert-butyl-4-hydroxy)benzoate,tetradecyl(3,5-di-tert-butyl-4-hydroxy)benzoate,hexadecyl(3,5-di-tert-butyl-4-hydroxy)benzoate,octadecyl(3,5-di-tert-butyl-4-hydroxy)benzoate andbehenyl(3,5-di-tert-butyl-4-hydroxy)benzoate; substituted oxanilidessuch as 2-ethyl-2′-ethoxyoxanilide and 2-ethoxy-4′-dodecyloxanilide;cyanoacrylates such as ethyl-α-cyano-β,β-diphenylacrylate andmethyl-2-cyano-3-methyl-3-(p-methoxyphenyl)acrylate; and various metalsalts and metal chelates, especially salts and chelates of nickel andchrome.

The amount of the ultraviolet absorber used is preferably 0.001 to 5parts by mass, more preferably 0.005 to 0.5 part by mass with respect to100 parts by mass of the olefin polymer.

Examples of the hindered amine light stabilizers include2,2,6,6-tetramethyl-4-piperidylstearate,1,2,2,6,6-pentamethyl-4-piperidylstearate,2,2,6,6-tetramethyl-4-piperidylbenzoate,bis(2,2,6,6-tetramethyl-4-piperidyl)sebacate,tetrakis(2,2,6,6-tetramethyl-4-piperidyl)-1,2,3,4-butanetetracarboxylate,tetrakis(1,2,2,6,6-pentamethyl-4-piperidyl)-1,2,3,4-butanetetracarboxylate,bis(2,2,6,6-tetramethyl-4-piperidyl).di(tridecyl)-1,2,3,4-butanetetracarboxylate,bis(1,2,2,6,6-pentamethyl-4-piperidyl).di(tridecyl)-1,2,3,4-butanetetracarboxylate,bis(1,2,2,4,4-pentamethyl-4-piperidyl)-2-butyl-2-(3,5-di-tert-butyl-4-hydroxybenzyl)malonate,1-(2-hydroxyethyl)-2,2,6,6-tetramethyl-4-piperidinol/diethyl succinatepolycondensate,1,6-bis(2,2,6,6-tetramethyl-4-piperidylamino)hexane/2,4-dichloro-6-morpholino-s-triazinepolycondensate,1,6-bis(2,2,6,6-tetramethyl-4-piperidylamino)hexane/2,4-dichloro-6-tert-octylamino-s-triazinepolycondensate,1,5,8,12-tetrakis[2,4-bis(N-butyl-N-(2,2,6,6-tetramethyl-4-piperidyl)amino)-s-triazin-6-yl]-1,5,8,12-tetraazadodecane,1,5,8,12-tetrakis[2,4-bis(N-butyl-N-(1,2,2,6,6-pentamethyl-4-piperidyl)amino)-s-triazin-6-yl]-1,5,8-12-tetraazadodecane,1,6,11-tris[2,4-bis(N-butyl-N-(2,2,6,6-tetramethyl-4-piperidyl)amino)-s-triazin-6-yl]aminoundecane,1,6,11-tris[2,4-bis(N-butyl-N-(1,2,2,6,6-pentamethyl-4-piperidyl)amino)-s-triazin-6-yl]aminoundecane,bis[4-(1-octyloxy-2,2,6,6-tetramethyl)piperidyl]decanedionate,bis[4-(2,2,6,6-tetramethyl-1-undecyloxy)piperidyl]carbonate, and TINUVINNOR 371 manufactured by Ciba Specialty Chemicals K.K.

The amount of the hindered amine light stabilizer to be used ispreferably 0.001 to 5 parts by mass, more preferably 0.005 to 0.5 partby mass with respect to 100 parts by mass of the olefin polymer.

Examples of the nucleating agents include metal salts of carboxylicacids such as sodium benzoate, aluminum 4-tert-butyl benzoate, sodiumadipate and disodium bicyclo[2.2.1]heptane-2,3-dicarboxylate; phosphoricester metal salts such as sodium bis(4-tert-butylphenyl)phosphate,sodium-2,2′-methylenebis(4,6-di-tert-butylphenyl)phosphate andlithium-2,2′-methylenebis(4,6-di-tert-butylphenyl)phosphate; polyolderivatives such as dibenzylidene sorbitol,bis(methylbenzylidene)sorbitol, bis(p-ethylbenzylidene)sorbitol andbis(dimethylbenzylidene)sorbitol; and amide compounds such asN,N′,N″-tris[2-methylcyclohexyl]-1,2,3-propanetricarboxamide (RIKACLEARPC1), N,N′,N″-tricyclohexyl-1,3,5-benzenetricarboxamide,N,N′-dicyclohexyl-naphthalenedicarboxamide and1,3,5-tri(dimethylisopropylamino)benzene.

The amount of the nucleating agent to be used is preferably 0.001 to 10parts by mass, more preferably 0.005 to 5 parts by mass with respect to100 parts by mass of the olefin polymer.

Examples of the flame retardants include aromatic phosphates such astriphenyl phosphate, tricresyl phosphate, trixylenyl phosphate, cresyldiphenyl phosphate, cresyl-2,6-xylenyl phosphate and resorcinolbis(diphenylphosphate); phosphonates such as divinyl phenyl phosphonate,diallyl phenyl phosphonate and (1-butenyl)phenyl phosphonate;phosphinates such as phenyl diphenyl phosphinate, methyl diphenylphosphinate and 9,10-dihydro-9-oxa-10-phosphaphenanthrene-10-oxidederivatives; phosphazene compounds such asbis(2-allylphenoxy)phosphazene and dicresylphosphazene;phosphorus-containing flame retardants such as melamine phosphate,melamine pyrophosphate, melamine polyphosphate, melam polyphosphate,ammonium polyphosphate, phosphorus-containing vinylbenzyl compounds andred phosphorus; metal hydroxides such as magnesium hydroxide andaluminum hydroxide; bromine-containing flame retardants such asbrominated bisphenol A epoxy resins, brominated phenol novolac epoxyresins, hexabromobenzene, pentabromotoluene,ethylenebis(pentabromophenyl), ethylenebistetrabromophthalimide,1,2-dibromo-4-(1,2-dibromoethyl)cyclohexane, tetrabromocyclooctane,hexabromocyclododecane, bis(tribromophenoxy)ethane, brominatedpolyphenylene ether, brominated polystyrene and2,4,6-tris(tribromophenoxy)-1,3,5-triazine, tribromophenyl maleimide,tribromophenyl acrylate, tribromophenyl methacrylate,tetrabromobisphenol A dimethacrylate, pentabromobenzyl acrylate andbrominated styrene.

The amount of the flame retardant to be used is preferably 1 to 70 partsby mass, more preferably 10 to 30 parts by mass with respect to 100parts by mass of the olefin polymer.

Examples of the another phenolic antioxidant include2,6-di-tert-butyl-p-cresol, 2,6-diphenyl-4-octadecyloxyphenol,stearyl(3,5-di-tert-butyl-4-hydroxyphenyl)propionate,distearyl(3,5-di-tert-butyl-4-hydroxybenzyl)phosphonate,tridecyl-3,5-di-tert-butyl-4-hydroxybenzylthioacetate,thiodiethylene-bis[(3,5-di-tert-butyl-4-hydroxyphenyl)propionate],4,4′-thio-bis(6-tert-butyl-m-cresol),2-octylthio-4,6-di(3,5-di-tert-butyl-4-hydroxyphenoxy)-s-triazine,2,2′-methylene-bis(4-methyl-6-tert-butylphenol),bis[3,3-bis(4-hydroxy-3-tert-butylphenyl)butyric acid]glycol ester,4,4′-butylidene-bis(2,6-di-tert-butylphenol),4,4′-butylidene-bis(6-tert-butyl-3-methylphenol),2,2′-ethylidene-bis(4,6-di-tert-butylphenol),1,1,3-tris(2-methyl-4-hydroxy-5-tert-butylphenyl)butane,bis[2-tert-butyl-4-methyl-6-(2-hydroxy-3-tert-butyl-5-methylbenzyl)phenyl]terephthalate,1,3,5-tris(2,6-dimethyl-3-hydroxy-4-tert-butylbenzyl)isocyanurate,1,3,5-tris(3,5-di-tert-butyl-4-hydroxybenzyl)isocyanurate,1,3,5-tris(3,5-di-tert-butyl-4-hydroxybenzyl)-2,4,6-trimethylbenzene,1,3,5-tris[(3,5-di-tert-butyl-4-hydroxyphenyl)propionyloxyethyl]isocyanurate,tetrakis[methylene-3-(3′,5′-di-tert-butyl-4′-hydroxyphenyl)propionate]methane,2-tert-butyl-4-methyl-6-(2-acroyloxy-3-tert-butyl-5-methylbenzyl)phenol,3,9-bis[2-(3-tert-butyl-4-hydroxy-5-methylhydrocinnamoyloxy)-1,1-dimethylethyl]-2,4,8,10-tetraoxaspiro[5.5]undecaneand triethylene glycolbis[β-(3-tert-butyl-4-hydroxy-5-methylphenyl)propionate].

The amount of the another phenolic antioxidant to be used is preferably0.001 to 10 parts by mass, more preferably 0.01 to 5 parts by mass withrespect to 100 parts by mass of the olefin polymer.

The fiber obtained using a polyolefin powder of the present inventioncan be generally employed in uses wherein polyolefin fibers have beenconventionally employed, and examples of the uses include substrates forprinting; substrates for wallpapers; wiping materials; various filtermaterials; medical and sanitary materials such as stupe materials andsanitary products; clothing; interlining for clothing; pillowcases;decorative substrates; automotive interior materials; sound absorbingmaterials; packaging materials; and industrial materials such as thosefor engineering works.

EXAMPLES

The present invention will be described in more detail by way of theProduction Examples, Examples, Comparative Examples and EvaluationExamples below, but the present invention is not restricted by theseExamples and the like. The Production Examples are examples of themethod for producing an olefin polymer which is obtained bypolymerization of olefin monomers, and the Examples are examples of themethod of recycling of a phenolic antioxidant, which is masked by anorganoaluminum compound and contained in an olefin polymer, into aphenolic body.

Production Example 1 Bulk Polymerization

According to the following procedure ([1] preparation of a catalystslurry, [2] masking treatment of a phenolic antioxidant, and [3]polymerization of olefin monomers), an olefin polymer was obtained bybulk polymerization.

[1] Preparation of Catalyst Slurry

A homogeneous solution was prepared by mixing 4.76 g (50 mmol) ofanhydrous magnesium chloride, 25 mL of decane and 23.4 mL (150 mmol) of2-ethylhexyl alcohol together and allowing the reaction to proceed underheat at 130° C. for 2 hours. This was followed by addition of 1.11 g(7.5 mmol) of phthalic anhydride to the homogeneous solution andstirring the resulting mixture for 1 hour while maintaining atemperature of 130° C., to dissolve the phthalic anhydride in thehomogeneous solution. Subsequently, the homogeneous solution was cooledto room temperature, and its total amount was fed dropwise to 200 mL(1.8 mol) of titanium tetrachloride kept at −20° C., for 1 hour. Aftercompletion of the feeding, the temperature was increased to 110° C. for4 hours. When the temperature reached 110° C., 2.68 mL (12.5 mmol) ofdiisobutyl phthalate was added, and the resulting mixture was stirredfor 2 hours while the temperature of 110° C. was maintained, to allowthe reaction to proceed. After completion of the reaction, hotfiltration was carried out to collect the residue, and the residue wasresuspended in 200 mL of titanium tetrachloride, followed by heating theresulting suspension again to 110° C. and then allowing the reaction toproceed for 2 hours. After completion of the reaction, hot filtrationwas carried out again to collect the residue, and the residue was washedsufficiently with decane and hexane at 110° C. until free titaniumcompounds in the washing liquid became undetectable, to obtain a solidtitanium catalyst component. An aliquot of the solid titanium catalystcomponent was dried and subjected to analysis of the catalystcomposition, and, as a result, the composition was turned out to be 3.1%by weight titanium, 56.0% by weight chlorine, 17.0% by weight magnesiumand 20.9% by weight isobutyl phthalate.

To the solid titanium catalyst component synthesized by the aboveproduction method, heptane was added such that a concentration of 5mg/mL was achieved as a slurry in heptane, to prepare a catalyst slurry.

[2] Masking Treatment of Phenolic Antioxidant

To 50 mL of a container wherein the atmosphere was replaced withnitrogen, 18 g of heptane, 3 g (0.026 mol) of triethylaluminum and, as aphenolic antioxidant, 9 g of the above-described Compound No. 4 wereadded, to prepare a stabilizer solution containing a masked phenolicantioxidant.

[3] Polymerization of Olefin Monomers (Bulk Polymerization)

In a 1000-mL pressure-resistant reactor wherein the atmosphere wasreplaced with nitrogen, 35.4 mg of triethylaluminum, 33.3 mg of thestabilizer solution prepared in the above [2], 30 mg of aphosphorus-containing antioxidant:tris(2,4-di-tert-butylphenyl)phosphite, 7.08 mg (0.031 mmol) ofdicyclopentyldimethoxysilane and the catalyst slurry prepared in theabove [1] (0.0021 mmol in terms of the titanium component) were mixedtogether, and the resulting mixture was stirred for 2 minutes.

After replacing the atmosphere in the pressure-resistant reactor withpropylene, hydrogen was fed to the reactor to a hydrogen pressure of 0.2bar G, while the total pressure was kept at 38.2 bar G by continuouslyintroducing propylene into the pressure-resistant reactor, therebyperforming prepolymerization at 25° C. for 3 minutes. Thereafter, whilethe propylene pressure was maintained at 38.2 bar G, the temperature wasincreased to 70° C. and polymerization reaction was performed for 1hour. After completion or the reaction, the polymer containing thesolvent was transferred into a cylindrical container wherein theatmosphere was replaced with nitrogen, and the solvent was transferredto a flare line for solvent removal, to obtain the olefin polymer 1 aswhite solids.

Production Example 2 Gas-phase Polymerization

According to the following procedure ([1] preparation of a catalystslurry, [2] masking treatment of a phenolic antioxidant, and [3]polymerization of olefin monomers), the olefin polymer 2 was obtained.

[1] Preparation of Catalyst Slurry

A catalyst slurry was prepared in the same manner as in [1] in the aboveProduction Example 1.

[2] Masking Treatment of Phenolic Antioxidant

To 50 mL of heptane, 0.15 g (1.3 mmol) of triethylaluminum and, as aphenolic antioxidant, 10 mg of the above-described Compound No. 4 wereadded, and the resulting mixture was stirred for 2 hours, to performmasking treatment of the phenolic antioxidant.

[3] Polymerization of Olefin Monomers (Gas-phase Polymerization)

In a 1000-mL autoclave wherein the atmosphere was replaced withnitrogen, 400 mL of heptane was placed, and 0.148 g (1.3 mmol) oftriethylaluminum, 29.7 mg (0.13 mmol) of dicyclopentyldimethoxysilane,and the catalyst slurry prepared in the above [1] (0.12 mg in terms ofthe titanium component) were added thereto.

After replacing the atmosphere in the autoclave with propylene, apressure of 1 kgf/cm² G was applied with propylene, andprepolymerization was carried out at 35° C. for 10 minutes. Thereafter,propylene was purged to decrease the pressure, and 150 mL of hydrogen(23° C.) was then introduced, followed by increasing the temperature to60° C., supplying propylene into the autoclave such that a pressure of 5kgf/cm² G was achieved, and performing polymerization for 1 hour. Theobtained polymer was subjected twice to the following purification toobtain the olefin polymer 2.

(Purification)

After replacing the atmosphere with nitrogen, the polymer was left inthe autoclave, while heptane as the supernatant fluid was decanted.Heptane contained in the polymer was evaporated by evacuating theautoclave, to dry the polymer. In the autoclave, 10 g of the driedpolymer was left, and 44.5 mg (3.9 mmol) of triethylaluminum, 89 mg(0.39 mmol) of dicyclopentyldimethoxysilane, the catalyst slurryprepared in [1] (0.37 mg in terms of the titanium component), and 30 mgof a phosphorus-containing antioxidant:tris(2,4-di-tert-butylphenyl)phosphite were added thereto.

After replacing the atmosphere with propylene, propylene was purged todecrease the pressure, and 150 mL of hydrogen (23° C.) was thenintroduced, followed by increasing the temperature to 70° C. whilekeeping the propylene pressure at 5 kgf/cm² G to perform gas-phasepolymerization for 1 hour, to purity the polymer.

Example 1-1

A commercially available high-purity nitrogen gas was passed throughwater, to obtain a nitrogen gas having a moisture content of 1.2×10⁻³ interms of the volume ratio with respect to 1 volume of nitrogen.

Subsequently, the olefin polymer 1 obtained in the above ProductionExample 1 was transferred, with the solvent contained therein, to apurge column, and the solvent was transferred under nitrogen atmosphereto a flare line for solvent removal. With the olefin polymer afterremoval of the solvent, the above-described nitrogen gas was broughtinto contact by flowing the nitrogen gas from the bottom of thecylindrical container at a flow rate of 100 mL/min. for 5 hours, toperform recycling treatment of the masked phenolic antioxidant containedin the olefin polymer.

Example 1-2

Example 1-2 was carried out in the same manner as the above Example 1-1except that a nitrogen gas having a moisture content of 1.0×10⁻² interms of the volume ratio with respect to 1 volume of nitrogen was usedinstead of the nitrogen gas having a moisture content of 1.2×10⁻³ interms of the volume ratio with respect to 1 volume of nitrogen.

Comparative Example 1-1

Comparative Example 1-1 was carried out in the same manner as the aboveExample 1-1 except that a nitrogen gas having a moisture content of5.3×10⁻² in terms of the volume ratio with respect to 1 volume ofnitrogen was used instead of the nitrogen gas having a moisture contentof 1.2×10⁻³ in terms of the volume ratio with respect to 1 volume ofnitrogen.

Comparative Example 1-2

Comparative Example 1-2 was carried out in the same manner as the aboveExample 1-1 except that a nitrogen gas having a moisture content of2.7×10⁻² in terms of the volume ratio with respect to 1 volume ofnitrogen was used instead of the nitrogen gas having a moisture contentof 1.2×10⁻³ in terms of the volume ratio with respect to 1 volume ofnitrogen.

Comparative Example 1-3

The olefin polymer 1 obtained in the above Production Example 1 wastransferred, with the solvent contained therein, to a purge column, andthe solvent was transferred under nitrogen atmosphere to a flare linefor solvent removal. Subsequently, steam at 5 kPa was brought intocontact with the polymer at a flow rate of 100 mL/min. from the lowerside of the column on the cylinder of the purge column.

Reference Example 1

The olefin polymer with which steam was brought into contact in theabove Comparative Example 1-3 was dried at 40° C. for 5 hours.

(Evaluation of Stabilization Effect)

In terms of the olefin polymers obtained in Production Example 1, eachof the olefin polymers obtained by the methods of the above Examples 1-1and 1-2 and Comparative Examples 1-1 to 1-3 was processed into pelletsby granulation using a uniaxial extruder (apparatus: Plastomill μ,manufactured by Toyo Seiki Seisaku-sho, LTD.; extrusion temperature,230° C.; screw speed, 50 rpm). Based on the difference between theweight average molecular weights observed before and after thegranulation, the stabilization effect of each olefin polymer wasevaluated.

The weight average molecular weights were measured by gel permeationchromatography (apparatus: GPC 2000, manufactured by Waters Corporation;columns: 2 columns of Styragel HT 6E and 1 column of Styragel HT2,manufactured by Waters Corporation; measurement temperature: 135° C.;solvent: o-dichlorobenzene; concentration: 6 mg/10 g).

In the above (Evaluation of Stabilization Effect), presence/absence ofbubbling was confirmed upon the extrusion.

The respective results are shown in Table 1 below.

TABLE 1 Evaluation of stabilization effect Proton donor Weight averagemolecular weight of Method of [volume ratio olefin polymer, Mw × 10⁵production of with respect to Before After olefin polymer Fluidnitrogen] granulation granulation Bubbling Example Bulk NitrogenMoisture 4.02 4.05 No 1-1 polymerization gas 1.2 × 10⁻³ Example BulkNitrogen Moisture 3.99 4.01 No 1-2 polymerization gas 1.0 × 10⁻²Comparative Bulk Nitrogen Moisture 4.06 3.55 No Example 1-1polymerization gas 5.3 × 10⁻⁷ Comparative Bulk Nitrogen Moisture 4.084.05 Yes Example 1-2 polymerization gas 2.7 × 10⁻² Comparative BulkSteam — 4.03 4.06 Yes Example 1-3 polymerization Reference Bulk Steam —4.10 4.08 No Example 1* polymerization Reference Example 1*: AfterComparative Example 1-3, a drying step was carried out at 40° C. for 5hours.

As is evident from the results of Comparative Example 1-1 in Table 1,the treatment with a nitrogen gas having a moisture content of less than1.0×10⁻⁶ in terms of the volume ratio with respect to 1 volume ofnitrogen resulted in insufficient recycling of the phenolic antioxidantcontained in the olefin polymer, and the molecular weight of the olefinpolymer drastically decreased. Further, as is evident from the resultsof Comparative Example 1-2, in cases where the treatment was carried outwith a nitrogen gas having a moisture content of more than 1.5×10⁻³ interms of the volume ratio with respect to 1 volume of nitrogen, and, asis evident from the results of Comparative Example 1-3, in cases wherethe treatment was carried out with steam, although a sufficientstabilization effect could be obtained, the water content of the olefinpolymer was too much, leading to unstable production due to bubblingduring the granulation process.

In contrast, by recycling of the phenolic antioxidant by the method ofthe present invention, an olefin polymer having an excellentstabilization effect could be obtained.

Although, as shown in Reference Example 1, the problem of bubblingduring the granulation process, which occurs in cases where thetreatment with steam was carried out, can be solved by introduction of astep of drying of the olefin polymer, a drying apparatus is additionallyrequired and hence more equipment investment is necessary, which isindustrially disadvantageous compared to the method of the presentinvention.

Example 2-1

A commercially available high-purity nitrogen gas was passed throughwater, to obtain a nitrogen gas having a moisture content of 1.2×10⁻³ interms of the volume ratio with respect to 1 volume of nitrogen.

Subsequently, the olefin polymer 2 obtained in the above ProductionExample 2 was transferred, with the solvent contained therein, from theupper part of an upright cylindrical container wherein the atmospherewas replaced with nitrogen, and a nitrogen gas having a moisture contentof 1.2×10⁻³ (in terms of the volume ratio with respect to nitrogen) wasflown from the lower part of the cylindrical container at a flow rate of100 mL/min. for 1 hour, to perform recycling treatment of the maskedphenolic antioxidant contained in the olefin polymer 2.

Example 2-2

Example 2-2 was carried out in the same manner as in the above Example2-1 except that a nitrogen gas having a moisture content of 1.0×10⁻² (interms of the volume ratio with respect to nitrogen) was used instead ofthe nitrogen gas having a moisture content of 1.2×10⁻³ (in terms of thevolume ratio with respect to nitrogen).

Example 2-3

Example 2-3 was carried out in the same manner as the above Example 2-1except that methanol was used instead of water.

Example 2-4

Example 2-4 was carried out in the same manner as the above Example 2-1except that ethanol was used instead of water.

Comparative Example 2-1

Comparative Example 2-1 was carried out in the same manner as the aboveExample 2-1 except that a nitrogen gas having a moisture content of5.3×10⁻⁷ in terms of the volume ratio with respect to 1 volume ofnitrogen was used instead of the nitrogen gas having a moisture contentof 1.2×10⁻³ in terms of the volume ratio with respect to 1 volume ofnitrogen.

Comparative Example 2-2

Comparative Example 2-2 was carried out in the same manner as the aboveExample 2-1 except that a nitrogen gas having a moisture content of2.7×10⁻² in terms of the volume ratio with respect to 1 volume ofnitrogen was used instead of the nitrogen gas having a moisture contentof 1.2×10⁻³ in terms of the volume ratio with respect to 1 volume ofnitrogen.

Comparative Example 2-3

The olefin polymer 2 obtained in the above Production Example 2 wastransferred, with the solvent contained therein, to a purge column, andthe solvent was transferred under nitrogen atmosphere to a flare linefor solvent removal. Subsequently, steam at a pressure of 5 kPa wasbrought into contact with the polymer at a flow rate of 100 mL/min. fromthe lower side of the column on the cylinder of the purge column.

Reference Example 2

The olefin polymer with which steam was brought into contact in theabove Comparative Example 2-3 was dried at 40° C. for 5 hours.

(Evaluation of Stabilization Effect)

Each of the olefin polymers obtained in the above Examples andComparative Examples was processed into pellets by granulation using auniaxial extruder (apparatus: Plastomill μ, manufactured by Toyo SeikiSeisaku-sho, LTD.; extrusion temperature, 230° C.; screw speed, 50 rpm),and, based on the difference between the weight average molecularweights observed before and after the extrusion, the stabilizationeffect of each olefin polymer was evaluated.

The weight average molecular weights were measured by gel permeationchromatography (apparatus: GPC 2000, manufactured by Waters Corporation;columns: 2 columns of Styragel HT 6E and 1 column of Styragel HT2,manufactured by Waters Corporation; measurement temperature: 145° C.;solvent: o-dichlorobenzene; concentration: 4 mg/10 g).

Further, in the evaluation of the stabilization effect, presence/absenceof bubbling was confirmed upon the extrusion of pellets.

The respective results are shown in Table 2 below.

TABLE 2 Evaluation of stabilization effect Proton donor Weight averagemolecular weight of Method of [volume ratio olefin polymer, Mw × 10⁵production of with respect to Before After olefin polymer Fluidnitrogen] granulation granulation Bubbling Example 2-1 Gas-phaseNitrogen Moisture 3.66 3.64 No polymerization gas 1.2 × 10⁻³ Example 2-2Gas-phase Nitrogen Moisture 3.49 3.53 No polymerization gas 1.0 × 10⁻²Example 2-3 Gas-phase Nitrogen Methanol 3.52 3.51 No polymerization gasExample 2-4 Gas-phase Nitrogen Ethanol 3.60 3.57 No polymerization gasComparative Gas-phase Nitrogen Moisture 3.58 2.85 No Example 2-1polymerization gas 5.3 × 10⁻⁷ Comparative Gas-phase Nitrogen Moisture3.58 3.58 Yes Example 2-2 polymerization gas 2.7 × 10⁻² ComparativeGas-phase Steam — 3.61 3.58 Yes Example 2-3 polymerization ReferenceGas-phase Steam — 3.71 3.68 No Example 2* polymerization ReferenceExample 2*: After Comparative Example 2-3, a drying step was carried outat 40° C. for 5 hours.

As shown by the results of Comparative Example 2-1 in Table 2, thetreatment with a nitrogen gas having a moisture content of less than1.0×10⁻⁶ in terms of the volume ratio with respect to 1 volume ofnitrogen resulted in insufficient recycling of the phenolic antioxidantcontained in the olefin polymer, and the molecular weight of the olefinpolymer drastically decreased. Further, as shown by the results ofComparative Example 2-2, in cases where the treatment was carried outwith a nitrogen gas having a moisture content of more than 2.5×10⁻² interms of the volume ratio with respect to 1 volume of nitrogen, and, asis evident from the results of Comparative Example 2-3, in cases wherethe treatment was carried out with steam, although a sufficientstabilization effect could be obtained, the water content of the olefinpolymer was too much, leading to unstable production due to bubblingduring the granulation process.

In contrast, by recycling of the phenolic antioxidant by the method ofthe present invention, an olefin polymer having an excellentstabilization effect could be obtained.

Further, by Examples 2-3 and 2-4, it was confirmed that the effect ofthe present invention can be obtained also by using, as an alternativeto moisture, a proton donor such as methanol or ethanol.

Although, as shown in Reference Example 2, the problem of bubblingduring granulation, which occurs in cases where the treatment with steamwas carried out, can be solved by introduction of a step of drying ofthe olefin polymer, it is industrially disadvantageous, compared to themethod of the present invention, to newly introduce the drying stepsince there may be restriction of the space for installation of a dryingapparatus and more equipment investment may be required.

Production Example 3 Slurry Polymerization

According to the following procedure ([1] preparation of a catalystslurry, [2] masking treatment of a phenolic antioxidant, and [3]polymerization of olefin monomers), the olefin polymer 3 was obtained byslurry polymerization.

[1] Preparation of Catalyst Slurry

A homogeneous solution was prepared by mixing 4.76 g (50 mmol) ofanhydrous magnesium chloride, 25 mL of decane and 23.4 mL (150 mmol) of2-ethylhexyl alcohol together and allowing the reaction to proceed underheat at 130° C. for 2 hours. This was followed by addition of 1.11 g(7.5 mmol) of phthalic anhydride to the homogeneous solution andstirring the resulting mixture for 1 hour while maintaining atemperature of 130° C., to dissolve the phthalic anhydride in thehomogeneous solution. Subsequently, the homogeneous solution was cooledto room temperature, and its total amount was fed dropwise to 200 mL(1.8 mol) of titanium tetrachloride kept at −20° C., for 1 hour. Aftercompletion of the feeding, the temperature was increased to 110° C. for4 hours. When the temperature reached 110° C., 2.68 mL (12.5 mmol) ofdiisobutyl phthalate was added, and the resulting mixture was stirredfor 2 hours while the temperature of 110° C. was maintained, to allowthe reaction to proceed. After completion of the reaction, hotfiltration was carried out to collect the residue, and the residue wasresuspended in 200 mL of titanium tetrachloride, followed by heating theresulting suspension again to 110° C. and then allowing the reaction toproceed for 2 hours. After completion of the reaction, hot filtrationwas carried out again to collect the residue, and the residue was washedsufficiently with decane and hexane at 110° C. until free titaniumcompounds in the washing liquid became undetectable, to obtain a solidtitanium catalyst component. An aliquot of the solid titanium catalystcomponent was dried and subjected to analysis of the catalystcomposition, and, as a result, the composition was turned out to be 3.1%by weight titanium, 56.0% by weight chlorine, 17.0% by weight magnesiumand 20.9% by weight isobutyl phthalate.

To the solid titanium catalyst component synthesized by the aboveproduction method, heptane was added such that a concentration of 5mg/mL was achieved as a slurry in heptane, to prepare a catalyst slurry.

[2] Masking Treatment of Phenolic Antioxidant

To 50 mL of toluene, 3 g of triisobutylaluminum and, as a phenolicantioxidant, 2 g of the above-described Compound No. 4 were added, andthe resulting mixture was stirred for 2 hours at room temperature, toobtain a stabilizer solution containing a masked phenolic antioxidant.

[3] Polymerization of Olefin Monomers

In a 1000-mL autoclave wherein the atmosphere was replaced withnitrogen, 400 mL of heptane, 30 mg of a phosphorus-containingantioxidant: tris(2,4-di-tert-butylphenyl)phosphite, and 50 mL of thestabilizer solution obtained by the masking treatment of the phenolicantioxidant in the above-described [2] were placed, and the resultingmixture was stirred at 23° C. for 5 minutes. Further, 1.14 g (5.0 mmol)of dicyclopentyldimethoxysilane and the catalyst slurry prepared in theabove-described [1] (5 mmol in terms of the titanium component) wereadded to the mixture, and the resulting mixture was stirred for 2minutes.

After replacing the atmosphere in the autoclave with propylene,prepolymerization was carried out at a propylene pressure of 1 kgf/cm² Gat 35° C. for 10 minutes. Thereafter, propylene was purged, and 150 mLof hydrogen (23° C.) was introduced to the autoclave, followed byapplying a pressure of 5 kgf/cm² G with propylene, increasing thetemperature to 70° C., and performing polymerization for 1 hour whilemaintaining the pressure.

Thereafter, the atmosphere in the autoclave was replaced with nitrogen,and the solvent was evaporated, to obtain the olefin polymer 3.

Example 3-1

The olefin polymer 3 obtained in the above Production Example 3 wassubjected to granulation using a biaxial extruder (apparatus: PCM-30,manufactured by Ikegai Corp.; extrusion temperature, 230° C.; screwspeed, 50 rpm). The granulation was carried out under nitrogenatmosphere until the olefin polymer 3 was fed into the biaxial extruder,and, under suction through vents in the vicinity of the head portion andin the vicinity of the central portion of the screw of the biaxialextruder, steam was injected into the barrel at a pressure of 15 kPa anda flow rate of 100 mL/min. between the feed inlet of the olefin polymer1 and the vents, to obtain pellets.

Example 3-2

Example 3-2 was carried out in the same manner as Example 3-1 exceptthat, instead of steam, a nitrogen gas having a moisture content of 0.1%in terms of the volume ratio with respect to nitrogen was introduced ata flow rate of 100 mL/min., to obtain pellets.

Comparative Example 3-1

Comparative Example 3-1 was carried out in the same manner as the aboveExample 3-1 except that the introduction of steam and the suctionthrough vents were not carried out during granulation of the olefinpolymer, to obtain pellets.

Production Example 4 Bulk Polymerization

According to the following procedure ([1] preparation of a catalystslurry, [2] masking treatment of a phenolic antioxidant, and [3]polymerization of olefin monomers), the olefin polymer 4 was obtained bybulk polymerization.

[1] Preparation of Catalyst Slurry

A homogeneous solution was prepared by mixing 4.76 g (50 mmol) ofanhydrous magnesium chloride, 25 mL of decane and 23.4 mL (150 mmol) of2-ethylhexyl alcohol together and allowing the reaction to proceed underheat at 130° C. for 2 hours. This was followed by addition of 1.11 g(7.5 mmol) of phthalic anhydride to the homogeneous solution andstirring the resulting mixture for 1 hour while maintaining thetemperature of 130° C., to dissolve the phthalic anhydride in thehomogeneous solution. Subsequently, the homogeneous solution was cooledto room temperature, and its total amount was fed dropwise to 200 mL(1.8 mol) of titanium tetrachloride kept at −20° C., for 1 hour. Aftercompletion of the feeding, the temperature was increased to 110° C. for4 hours. When the temperature reached 110° C., 2.68 mL (12.5 mmol) ofdiisobutyl phthalate was added, and the resulting mixture was stirredfor 2 hours while the temperature of 110° C. was maintained, to allowthe reaction to proceed. After completion of the reaction, hotfiltration was carried out to collect the residue, and the residue wasresuspended in 200 mL of titanium tetrachloride, followed by heating theresulting suspension again to 110° C. and then allowing the reaction toproceed for 2 hours. After completion of the reaction, hot filtrationwas carried out again to collect the residue, and the residue was washedsufficiently with decane and hexane at 110° C. until free titaniumcompounds in the washing liquid became undetectable, to obtain a solidtitanium catalyst component. An aliquot of the solid titanium catalystcomponent was dried and subjected to analysis of the catalystcomposition, and, as a result, the composition was turned out to be 3.1%by weight titanium, 56.0% by weight chlorine, 17.0% by weight magnesiumand 20.9% by weight isobutyl phthalate.

To the solid titanium catalyst component synthesized by the aboveproduction method, heptane was added such that a concentration of 5mg/mL was achieved as a slurry in heptane, to prepare a catalyst slurry.

[2] Masking Treatment of Phenolic Antioxidant

To 50 mL of toluene, 3 g of triisobutylaluminum and, as a phenolicantioxidant, 2 g of the above-described Compound No. 4 were added, andthe resulting mixture was stirred for 2 hours at room temperature, toobtain a stabilizer solution containing a masked phenolic antioxidant.

[3] Polymerization of Olefin Monomers

In a 2000-mL pressure-resistant reactor wherein the atmosphere wasreplaced with nitrogen, 40 mg (0.35 mmol) of triethylaluminum, 0.25 mLof the stabilizer solution obtained by the masking treatment of aphenolic antioxidant in the above [2], 30 mg of a phosphorus-containingantioxidant: tris(2,4-di-tert-butylphenyl)phosphite, 7.08 mg (0.031mmol) of dicyclopentyldimethoxysilane and the catalyst slurry preparedin the above [1] (0.021 mmol in terms of the titanium component) wereplaced, and the resulting mixture was stirred for 2 minutes.

After replacing the atmosphere in the pressure-resistant reactor withpropylene, propylene was continuously introduced while hydrogen was keptat a hydrogen pressure of 0.2 bar G and propylene was kept to achieve atotal pressure of 38.2 bar G, and prepolymerization was carried out at25° C. for 3 minutes. Thereafter, while the total pressure of propylenewas maintained at 38.2 bar G, the temperature was increased to 70° C.and polymerization reaction was performed for 1 hour. After completionor the reaction, the polymer containing the solvent was transferred intoa cylindrical container wherein the atmosphere had been replaced withnitrogen. The solvent was transferred to a flare line for solventremoval, to obtain the olefin polymer 4. The obtained olefin polymer wasstored as it is under nitrogen atmosphere.

Example 4-1

The olefin polymer 4 obtained in the above Production Example 4 wassubjected to granulation using a biaxial extruder (apparatus: PCM-30,manufactured by Ikegai Corp.; extrusion temperature, 230° C.; screwspeed, 50 rpm). The granulation was carried out under nitrogenatmosphere until the olefin polymer 4 was fed into the biaxial extruder,and, under suction through vents in the vicinity of the head portion andin the vicinity of the central portion of the screw of the biaxialextruder, steam was injected into the barrel at a pressure of 15 kPa anda flow rate of 100 mL/min. between the feed inlet of the olefin polymer4 and the vents, to obtain pellets.

Example 4-2

Example 4-2 was carried out in the same manner as Example 4-1 exceptthat, instead of steam, a nitrogen gas having a moisture content of 0.1%in terms of the volume ratio with respect to nitrogen was introduced ata flow rate of 100 mL/min., to obtain pellets.

Comparative Example 4-1

Comparative Example 4-1 was carried out in the same manner as Example4-1 except that the introduction of steam and the suction through ventswere not carried out during granulation, to obtain pellets.

Production Example 5 Gas-phase Polymerization

According to the following procedure ([1] preparation of a catalystslurry, [2] masking treatment of a phenolic antioxidant, and [3]polymerization of olefin monomers), the olefin polymer 5 was obtained bygas-phase polymerization.

[1] Preparation of Catalyst Slurry

A catalyst slurry, which is a slurry of a 5 mg/mL solid titaniumcatalyst component in heptane, was prepared in the same manner as in [1]in the above Production Example 3.

[2] Masking Treatment of Phenolic Antioxidant

To 50 mL of heptane, 3 g of triethylaluminum and, as a phenolicantioxidant, 2 g of the above-described Compound No. 4 were added, andthe resulting mixture was stirred for 2 hours, to obtain a stabilizersolution containing a masked phenolic antioxidant.

[3] Polymerization of Olefin Monomers (Gas-Phase Polymerization)

In a 1000-mL autoclave wherein the atmosphere was replaced withnitrogen, 400 mL of heptane was placed, and 148 mg (1.3 mmol) oftriethylaluminum, 29.7 mg (0.13 mmol) of dicyclopentyldimethoxysilane,and the catalyst slurry prepared in the above [1] (0.0026 mmol in termsof the Ti component) were added thereto.

After replacing the atmosphere in the autoclave with propylene, apressure of 1 kgf/cm² G was applied with propylene, andprepolymerization was carried out at 35° C. for 10 minutes. Thereafter,propylene was purged to decrease the pressure, and 150 mL of hydrogen(23° C.) was then introduced, followed by increasing the temperature to60° C., supplying propylene into the autoclave such that a totalpressure of 5 kgf/cm² G was maintained, increasing the temperature to70° C. and performing polymerization for 1 hour. The obtained polymerwas subjected twice to the following purification to obtain the olefinpolymer 5.

(Purification Method)

After replacing the atmosphere in the autoclave with nitrogen, thepolymer was left in the autoclave, while heptane as the supernatantfluid was decanted. Heptane contained in the polymer was evaporated byevacuating the autoclave, to dry the polymer. In the autoclave, 10 g ofthe dried polymer was left, and 44.5 mg (3.9 mmol) of triethylaluminum,89 mg (0.39 mmol) of dicyclopentyldimethoxysilane, the catalyst slurryprepared in [1] (0.0078 mmol in terms of the titanium component), 0.25ml of the stabilizer solution prepared in [2], and 30 mg oftris(2,4-di-tert-butylphenyl)phosphite as a phosphorus-containingantioxidant were added thereto.

After replacing the atmosphere in the autoclave with propylene,propylene was purged to decrease the pressure, and 150 mL of hydrogen(23° C.) was then introduced, followed by supplying propylene into theautoclave to maintain a total pressure of 5 kgf/cm² G and increasing thetemperature to 70° C. to perform gas-phase polymerization for 1 hour, topurify the polymer 5 of interest.

Example 5-1

The olefin polymer 5 obtained in the above Production Example 5 wassubjected to granulation using a biaxial extruder (apparatus: TEX-30α,manufactured by The Japan Steel Works, LTD.; extrusion temperature, 230°C.; screw speed, 100 rpm). The granulation was carried out undernitrogen atmosphere until the olefin polymer 5 was fed into the biaxialextruder, and, under suction through vents in the vicinity of the headportion and in the vicinity of the central portion of the screw of thebiaxial extruder, steam was injected into the barrel at a pressure of 15kPa and a flow rate of 100 mL/min. between the feed inlet of the olefinpolymer 5 and the vents in the biaxial extruder, to obtain pellets.

Example 5-2

Example 5-2 was carried out in the same manner as Example 5-1 exceptthat, instead of steam, a nitrogen gas having a moisture content of 0.1%in terms of the volume ratio with respect to nitrogen was introduced ata flow rate of 100 mL/min., to obtain pellets.

Comparative Example 5-1

Comparative Example 5-1 was carried out in the same manner as the aboveExample 5-1 except that the introduction of steam and the suctionthrough vents were not carried out during granulation of the olefinpolymer 5, to obtain pellets.

(Evaluation of Stabilization Effect)

Each of the pellets obtained in the Examples and Comparative Exampleswas subjected to granulation using a uniaxial extruder (apparatus:Plastomill μ, manufactured by Toyo Seiki Seisaku-sho, LTD.; extrusiontemperature, 230° C.; screw speed, 50 rpm), and, based on the differencebetween the weight average molecular weights observed before and afterthe extrusion, the stabilization effect of the olefin polymer wasevaluated.

The weight average molecular weights were measured by gel permeationchromatography (apparatus: GPC 2000, manufactured by Waters Corporation;columns: 2 columns of Styragel HT 6E and 1 column of Styragel HT2,manufactured by Waters Corporation; measurement temperature: 145° C.;solvent: o-dichlorobenzene; concentration: 4 mg/10 g).

The evaluation results are shown in Table 3 below.

TABLE 3 Evaluation of stabilization Aftertreatment effect ContactingWeight average molecular with moisture- weight of olefin polymer, Methodof Steam containing Mw × 10⁵ production of injection upon nitrogen uponBefore After olefin polymer granulation granulation granulationgranulation Example 3-1 Slurry ◯ — 4.03 4.06 polymerization Example 3-2Slurry — ◯ 4.02 3.98 polymerization Comparative Slurry — — 4.10 3.60Example 3-1 polymerization Example 4-1 Bulk ◯ — 4.08 4.10 polymerizationExample 4-2 Bulk — ◯ 4.11 4.03 polymerization Comparative Bulk — — 4.043.59 Example 4-1 polymerization Example 5-1 Gas-phase ◯ — 3.87 3.82polymerization Example 5-2 Gas-phase — ◯ 3.91 3.89 polymerizationComparative Gas-phase — — 3.76 3.17 Example 5-1 polymerization

As is evident from the results of Comparative Examples 3-1 to 5-1 inTable 3, a sufficient stabilization effect could not be obtained for theolefin polymers produced without using the method of the presentinvention, and their weight average molecular weights drasticallydecreased after the extrusion. In contrast, drastic decrease in theweight average molecular weight was not observed for the olefin polymersobtained by the production method of the present invention, and it wastherefore confirmed that a sufficient stabilization effect was obtainedby the production method of the present invention.

From the above results, it was confirmed that the effect of the presentinvention can be obtained, upon the granulation process of the olefinpolymer in an extruder, by injection of steam, or a nitrogen gascontaining moisture into the extruder.

(Preparation of Catalyst Slurry)

A homogeneous solution was prepared by mixing 4.76 g (50 mmol) ofanhydrous magnesium chloride, 25 mL of decane and 23.4 mL (150 mmol) of2-ethylhexyl alcohol together and allowing the reaction to proceed underheat at 130° C. for 2 hours. This was followed by addition of 1.11 g(7.5 mmol) of phthalic anhydride to the homogeneous solution andstirring the resulting mixture for 1 hour while maintaining atemperature of 130° C., to dissolve the phthalic anhydride in thehomogeneous solution. Subsequently, the homogeneous solution was cooledto room temperature, and its total amount was fed dropwise to 200 mL(1.8 mol) of titanium tetrachloride kept at −20° C., for 1 hour. Aftercompletion of the feeding, the temperature was increased to 110° C. for4 hours. When the temperature reached 110° C., 2.68 mL (12.5 mmol) ofdiisobutyl phthalate was added, and the resulting mixture was stirredfor 2 hours while the temperature of 110° C. was maintained, to allowthe reaction to proceed. After completion of the reaction, hotfiltration was carried out to collect the residue, and the residue wasresuspended in 200 mL of titanium tetrachloride, followed by heating theresulting suspension again to 110° C. and then allowing the reaction toproceed for 2 hours. After completion of the reaction, hot filtrationwas carried out again to collect the residue, and the residue was washedsufficiently with decane and hexane at 110° C. until free titaniumcompounds in the washing liquid became undetectable, to obtain a solidtitanium catalyst component. An aliquot of the solid titanium catalystcomponent was dried and subjected to analysis of the catalystcomposition, and, as a result, the composition was turned out to be 3.1%by weight titanium, 56.0% by weight chlorine, 17.0% by weight magnesiumand 20.9% by weight isobutyl phthalate.

To the solid titanium catalyst component synthesized by the aboveproduction method, heptane was added such that a concentration of 5mg/mL was achieved as a slurry in heptane, to prepare a catalyst slurry.

(Connection of Pipes)

In a production apparatus equipped with a supplying tank A for a slurryadditive containing a phenolic antioxidant, a supplying tank B fortriethylaluminum as a promoter and a polymerization tank C, a pipe 1 fortransfer of triethylaluminum from the supplying tank B to thepolymerization tank C was provided, and a pipe for transfer from thesupplying tank A to the pipe 1 was connected to the pipe 1.

Olefin monomers were polymerized by the following methods.

Examples 6-1 to 6-5

In the supplying tank A, a slurry additive was prepared as described inTable 4 below.

To the supplying tank B, 33.3 mg (0.29 mmol) of triethylaluminum wassupplied.

In the polymerization tank C, 29.7 mg (0.13 mmol) ofdicyclopentyldimethoxysilane, 445 mg (3.9 mmol) of triethylaluminum and0.0026 mmol of the catalyst slurry as a titanium component were placed.

Olefin monomers were polymerized as follows under the same conditionsexcept for the type of the slurry additive supplied to the supplyingtank.

(Polymerization Conditions)

At the same time as transfer of triethylaluminum from the supplying tankB to the polymerization tank C through the pipe 1, the slurry solutionwas transferred from the supplying tank A to the pipe 1, andtriethylaluminum and the slurry additive were thereby mixed together inthe pipe. The mixing in the pipe promptly caused the reaction to yield ahomogeneous composition, and the resulting reaction product was suppliedto the polymerization tank C. Immediately thereafter, the atmosphere inthe polymerization tank C was replaced with propylene, andprepolymerization was carried out under a pressure of propylene of 1kgf/cm² at 35° C. for 10 minutes. Thereafter, propylene was purged and150 mL of hydrogen (23° C.) was introduced, followed by introducingpropylene into the polymerization tank C to maintain a total pressure of5 kgf/cm² G, increasing the temperature to 70° C. and performingpolymerization for 1 hour. After replacing the atmosphere in thepolymerization tank C with nitrogen, 5 mL of ethanol was added theretoat 40° C. to stop the polymerization, and the solvent was removed underreduced pressure at 50° C., followed by performing drying treatment at40° C. for 5 hours while the vacuum state was maintained, to obtain anolefin polymer.

The composition of the slurry additive is shown in Table 4 below.

Comparative Example 6-1

In the supplying tank B for triethylaluminum, 10 mg of the aboveCompound No. 4 as a phenolic antioxidant, 30 mg oftris(2,4-di-tert-butylphenyl)phosphite as a phosphorus-containingantioxidant, 3.33 mg (0.029 mmol) of triethylaluminum and 60 mg ofheptane were preliminarily mixed together to form a slurry. However, byleaving the mixture to stand in the tank for 24 hours, gel was generatedthroughout the tank.

(Composition of Slurry Additive)

TABLE 4 Slurry additives Mixing Phosphorus- method for Phenoliccontaining additives and Generation antioxidant ¹⁾ antioxidant ²⁾Neutralizer ³⁾ Solvent ⁴⁾ promoter of gel Example 6-1 ◯ — — Heptane Inpipe No 60 mg Example 6-2 ◯ ◯ — Heptane In pipe No 60 mg Example 6-3 ◯ ◯◯ Heptane In pipe No 120 mg Example 6-4 ◯ ◯ — Hexane In pipe No 60 mgExample 6-5 ◯ ◯ — Cyclohexane In pipe No 60 mg Comparative ◯ ◯ — HeptanePreliminarily Yes Example 6-1 60 mg mixed in tank ¹⁾ Phenolicantioxidant: Compound No. 4 described above, 10 mg ²⁾Phosphorus-containing antioxidant:tris(2,4-di-tert-butylphenyl)phosphite, 30 mg ³⁾ Neutralizer: calciumstearate, 50 mg The additives ¹⁾ to ³⁾ were mixed with the solvent to bemade into a slurry additive.

In the above Comparative Example 6-1, preliminary mixing of anorganoaluminum as a promoter with the phenolic antioxidant and leavingof the resulting mixture for 1 day caused gelation throughout the tank.

In the above Comparative Example 6-1, in order for the phenolicantioxidant masked by the promoter organoaluminum compound to bemaintained as a homogeneous composition, equipment investment forproviding a blending tank or the like is necessary. Further, since anorganoaluminum compound is a compound which requires special care tosecure safety of its storage, continuous maintenance is required for along time.

Since, in some cases, polymerization of olefin monomers are continuedfor as long as several months, the tank for blending of a phenolicantioxidant and an organoaluminum compound needs to be provided inconsideration of both safety and scaling-up, but this requires highequipment investment, which is industrially disadvantageous.

In contrast, in the production method of the present invention, stablepolymerization of olefin monomers can be carried out with an existingpolymerization apparatus by just introducing a slurry additivecontaining a phenolic antioxidant into a pipe through which a promoterorganoaluminum compound is transferred to a polymerization tank, as canbe confirmed from the results of Examples 6-1 to 6-5 in Table 4.

Example 7-1

According to the following procedure ([1] preparation of a catalystslurry, [2] preparation of a phenoxide solution, [3] preparation of aphosphite solution, [4] polymerization of olefin monomers (propylenemonomers), and [5] preparation of a fiber), a fiber was obtained.

[1] Preparation of Catalyst Slurry

A homogeneous solution was prepared by mixing 4.76 g (50 mmol) ofanhydrous magnesium chloride, 25 mL of decane and 23.4 mL (150 mmol) of2-ethylhexyl alcohol together and allowing the reaction to proceed underheat at 130° C. for 2 hours. This was followed by addition of 1.11 g(7.5 mmol) of phthalic anhydride to the homogeneous solution andstirring the resulting mixture for 1 hour while maintaining atemperature of 130° C., to dissolve the phthalic anhydride in thehomogeneous solution. Subsequently, the homogeneous solution was cooledto room temperature, and its total amount was fed dropwise to 200 mL(1.8 mol) of titanium tetrachloride kept at −20° C., for 1 hour. Aftercompletion of the feeding, the temperature was increased to 110° C. for4 hours. When the temperature reached 110° C., 2.68 mL (12.5 mmol) ofdiisobutyl phthalate was added, and the resulting mixture was stirredfor 2 hours while the temperature of 110° C. was maintained, to allowthe reaction to proceed. After completion of the reaction, hotfiltration was carried out to collect the residue, and the residue wasresuspended in 200 mL of titanium tetrachloride, followed by heating theresulting suspension again to 110° C. and then allowing the reaction toproceed for 2 hours. After completion of the reaction, hot filtrationwas carried out again to collect the residue, and the residue was washedsufficiently with decane and hexane at 110° C. until free titaniumcompounds in the washing liquid became undetectable, to obtain a solidtitanium catalyst component. An aliquot of the solid titanium catalystcomponent was dried and subjected to analysis of the catalystcomposition, and, as a result, the composition was turned out to be 3.1%by weight titanium, 56.0% by weight chlorine, 17.0% by weight magnesiumand 20.9% by weight isobutyl phthalate.

To the solid titanium catalyst component synthesized by the aboveproduction method, heptane was added such that a concentration of 5mg/mL was achieved as a slurry in heptane, to prepare a catalyst slurry.

[2] Preparation of Phenoxide Solution

In a flask wherein the atmosphere was replaced with nitrogen, 1.03 g(1.94 mmol) of3-(3,5-di-tert-butyl-4-hydroxyphenyl)-N-octadecylpropionamide (the aboveCompound No. 4) and 65.5 mL of dry heptane were placed. With stirring,3.0 mL (1 mol/L) of triethylaluminum solution in heptane was addeddropwise thereto, to prepare a phenoxide solution.

[3] Preparation of Phosphite Solution

In a flask wherein the atmosphere was replaced with nitrogen, 0.9 g (1.4mmol) of tris(2,4-di-tert-butylphenyl)phosphite and 30 mL of dry heptanewere placed, to prepare a phosphite solution.

[4] Polymerization of Olefin Monomers (Propylene Monomers),

In an autoclave wherein the atmosphere was replaced with nitrogen, 600mL of dry heptane and 2.2 mL (1 mol/L) of triethylaluminum solution inheptane were placed. This was followed by sequential addition thereto of1.4 mL of the phenoxide solution prepared in the above [2], 0.7 mL ofthe phosphite solution prepared in the above [3], 4.1 mL of a heptanesolution prepared by dissolving 1.2 g (5.3 mmol) ofdicyclopentyldimethoxysilane in 100 mL of dry heptane, and 4.0 mL of thecatalyst slurry prepared in the above [1].

The atmosphere in the autoclave was replaced with propylene, andhydrogen (7.0 L; in terms of the volume in the standard state) was fedthereto, followed by performing prepolymerization (600 rpm) at apropylene pressure of 1 kgf/cm² G at 50° C. for 5 minutes. Thereafter,polymerization reaction was carried out at a propylene pressure of 6kgf/cm² at 70° C. for 1 hour. After purging the gas, 5 mL of ethanol wasadded to the reaction liquid, and the resulting mixture was stirred for5 minutes to stop the polymerization reaction, followed by removing thesolvent under reduced pressure and drying the resultant under vacuum at40° C. for 10 hours, to obtain a polypropylene powder prepared bypolymerizing propylene monomers.

[5] Preparation of Fiber

To 100 parts by mass of the obtained polypropylene powder, 0.05 part bymass of calcium stearate was added, and these were mixed together,followed by being subjected to granulation using a uniaxial extruder(apparatus: Plastomill μ, manufactured by Toyo Seiki Seisaku-sho, LTD.;extrusion temperature, 230° C.; screw speed, 50 rpm), to obtain pellets.The pellets were supplied to a spinning machine (30-mm diameter,manufactured by Shimadzu Corporation) and extruded into nozzles (0.45-mmdiameter, 230° C., 30 holes). A fiber was then collected at a windingrate of 1000 m/min. The obtained fiber was composed of 30 bundled6.8-denier filaments. Further, a sheet was prepared by pressing thepellets at 230° C. at a load of 120 kgf/cm² for 5 minutes. The thicknessof the sheet after the pressing was 2 mm.

Example 7-2

A fiber and a sheet were prepared in the same manner as in [3]Preparation of Phosphite Solution in the above Example 7-1 except that0.82 g (1.4 mmol) of2,2′-methylenebis(4,6-di-tert-butylphenyl)-octadecylphosphite was usedinstead of 0.90 g (1.4 mmol) of tris(2,4-di-tert-butylphenyl)phosphite.

Comparative Example 7-1

A propylene polymer was obtained in the same manner as in [4]Polymerization of Olefin Monomers in the above Example 7-1 except that1.4 mL of the phenoxide solution and 0.7 mL of the phosphite solutionwere not used.

With 100 parts by mass of the obtained propylene polymer, 0.05 part bymass each oftetrakis[3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionyloxymethyl]methane,tris(2,4-di-tert-butylphenyl)phosphite and calcium stearate was mixed,and the resulting mixture was subjected to granulation using a uniaxialextruder (apparatus: Plastomill μ, manufactured by Toyo SeikiSeisaku-sho, LTD.; extrusion temperature, 230° C.; screw speed, 50 rpm),to obtain pellets. The pellets were supplied to a spinning machine(30-mm diameter, manufactured by Shimadzu Corporation) and extruded intonozzles (0.45-mm diameter, 230° C., 30 holes). A fiber was thencollected at a winding rate of 1000 m/min. The obtained fiber wascomposed of 30 bundled 6.8-denier filaments. Further, a sheet wasprepared by pressing the pellets at 230° C. at a load of 120 kgf/cm² for5 minutes. The thickness of the sheet after the pressing was 2 mm.

Comparative Example 7-2

A propylene polymer was obtained in the same manner as in [4]Polymerization of Olefin Monomers in the above Example 7-1 except that1.4 mL of the phenoxide solution and 0.7 mL of the phosphite solutionwere not used. To 100 parts by mass of the obtained propylene polymer,0.01 part by mass each of1,3,5-tris(3-hydroxy-4-tert-butyl-2,6-dimethylbenzyl)isocyanurate and2,2′-methylenebis(4,6-di-tert-butylphenyl)-octadecylphosphite, and 0.05part by mass of calcium stearate were added, and the resulting mixturewas mixed well, followed by being subjected to granulation using auniaxial extruder (apparatus: Plastomill μ, manufactured by Toyo SeikiSeisaku-sho, LTD.; extrusion temperature, 230° C.; screw speed, 50 rpm),to obtain pellets. The pellets were supplied to a spinning machine(30-mm diameter, manufactured by Shimadzu Corporation) and extruded intonozzles (0.45-mm diameter, 230° C., 30 holes). A fiber was thencollected at a winding rate of 1000 m/min. The obtained fiber wascomposed of 30 bundled 6.8-denier filaments. Further, a sheet wasprepared by pressing the pellets at 230° C. at a load of 120 kgf/cm² for5 minutes. The thickness of the sheet after the pressing was 2 mm.

Comparative Example 7-3

A fiber and a sheet were produced in the same manner as in [4]Polymerization of Olefin Monomers in the above Example 7-1 except that2.8 mL, instead of 1.4 mL, of the phenoxide solution was used and 0.7 mLof the phosphite solution was not used.

Comparative Example 7-4

A fiber and a sheet were produced in the same manner as in [4]Polymerization of Olefin Monomers in the above Example 7-1 except that1.4 mL, instead of 0.7 mL, of the phenoxide solution was used and 1.4 mLof the phenoxide solution was not used.

Comparative Example 7-5

A propylene polymer was obtained in the same manner as in [4]Polymerization of Olefin Monomers in the above Example 7-1 except that1.4 mL of the phenoxide solution and 0.7 mL of the phosphite solutionwere not used. To 100 parts by mass of the obtained propylene polymer,0.01 part by mass each of Compound No. 4 andtris(2,4-di-tert-butylphenyl)phosphite, and 0.05 part by mass of calciumstearate were added, and the resulting mixture was mixed well, followedby being subjected to granulation using a uniaxial extruder (apparatus:Plastomill n, manufactured by Toyo Seiki Seisaku-sho, LTD.; extrusiontemperature, 230° C.; screw speed, 50 rpm), to obtain pellets. Thepellets were supplied to a spinning machine (30-mm diameter,manufactured by Shimadzu Corporation) and extruded into nozzles (0.45-mmdiameter, 230° C., 30 holes). A fiber was then collected at a windingrate of 1000 m/min. The obtained fiber was composed of 30 bundled6.8-denier filaments. Further, a sheet was prepared by pressing thepellets at 230° C. at a load of 120 kgf/cm² for 5 minutes. The thicknessof the sheet after the pressing was 2 mm.

Comparative Example 7-6

A propylene polymer was obtained in the same manner as in [4]Polymerization of Olefin Monomers in the above Example 7-1 except that1.4 mL of the phenoxide solution was not used. To 100 parts by mass ofthe obtained propylene polymer, 0.01 part by mass of the above CompoundNo. 4 and 0.05 part by mass of calcium stearate were added, and theresulting mixture was mixed well, followed by being subjected togranulation using a uniaxial extruder (apparatus: Plastomill μ,manufactured by Toyo Seiki Seisaku-sho, LTD.; extrusion temperature,230° C.; screw speed, 50 rpm), to obtain pellets. The pellets weresupplied to a spinning machine (30-mm diameter, manufactured by ShimadzuCorporation) and extruded into nozzles (0.45-mm diameter, 230° C., 30holes). A fiber was then collected at a winding rate of 1000 m/min. Theobtained fiber was composed of 30 bundled 6.8-denier filaments. Further,a sheet was prepared by pressing the pellets at 230° C. at a load of 120kgf/cm² for 5 minutes. The thickness of the sheet after the pressing was2 mm.

Comparative Example 7-7

A propylene polymer was obtained in the same manner as in [4]Polymerization of Olefin Monomers in the above Example 7-1 except that0.7 mL of the phosphite solution was not used. To 100 parts by mass ofthe obtained propylene polymer, 0.01 part by mass oftris(2,4-di-tert-butylphenyl)phosphite and 0.05 part by mass of calciumstearate were added, and the resulting mixture was mixed well, followedby being subjected to granulation using a uniaxial extruder (apparatus:Plastomill μ, manufactured by Toyo Seiki Seisaku-sho, LTD.; extrusiontemperature, 230° C.; screw speed, 50 rpm), to obtain pellets. Thepellets were supplied to a spinning machine (30-mm diameter,manufactured by Shimadzu Corporation) and extruded into nozzles (0.45-mmdiameter, 230° C., 30 holes). A fiber was then collected at a windingrate of 1000 m/min. The obtained fiber was composed of 30 bundled6.8-denier filaments. Further, a sheet was prepared by pressing thepellets at 230° C. at a load of 120 kgf/cm² for 5 minutes. The thicknessof the sheet after the pressing was 2 mm.

The fibers obtained in the above Examples 7-1 and 7-2, and ComparativeExamples 7-1 to 7-7 were subjected to the following evaluation of thestability. The respective results are shown in Table 5. In Table 5, thevalue shown below each compound name in the columns listing stabilizersrepresents the ratio of each stabilizer excluding the additivecomponent, with respect to 100 parts by mass of the propylene polymer.Further, the sheets obtained in the above Examples 7-1 and 7-2, andComparative Examples 7-1 to 7-7 were subjected to evaluation by a NOxgas color change test.

(NOx Gas Color Change Test)

A NOx gas color change test was carried out by the following procedure.The results are shown in Table 5 below.

A sheet was suspended on a glass rod and placed in a glass desiccator.

In a glass beaker, 9.52 g of 85% phosphoric acid was dissolved in 38.10g of distilled water to prepare an aqueous phosphoric acid solution, andthe beaker was placed in the glass desiccator.

In another glass beaker, 0.786 g of 97% sodium nitrate was dissolved in9.52 g of distilled water to prepare an aqueous sodium nitrate solution.

The aqueous sodium nitrate solution was added to the aqueous phosphoricacid solution in the glass desiccator at once, and the desiccator wasimmediately closed with a lid, to allow generation of 2% NOx gas.

The joint portion between the body and the lid of the glass desiccatorwas sealed with Valqua tape, and vinyl tape was further attachedthereto, to prevent gas leakage.

The glass desiccator was placed in a Geer oven at 40° C. and left tostand for 140 hours.

Thereafter, the yellowness index (YI) of the sheet was measured, todetermine the yellowness index for the sheet before the exposure to theNOx gas (initial Y. I.) and the yellowness index after the exposure test(AYI).

(Stability)

The fiber was left to stand at 120° C. in an oven for 15 hours, anddrawn by a tensile tester at a rate of 10 mm/min.

In the evaluation results, the symbols ◯, Δ, and X indicate degrees ofelongation of more than 200%, not less than 150% and not more than 200%,and less than 150%, respectively.

TABLE 5 Stabilizer Phosphorus- Evaluation Phenolic Method of containingMethod of Initial antioxidant addition ⁵⁾ antioxidant addition ⁵⁾ Y.I.ΔY.I. Stability ⁶⁾ Example 7-1 Compound A Compound 1¹⁾ A 1.2 4.3 ◯ No. 40.01 part by 0.01 part by mass mass Example 7-2 Compound A Compound 2²⁾A 1.0 4.0 ◯ No. 4 0.01 part by 0.01 part by mass mass ComparativeComparative B Compound 1¹⁾ B 2.1 9.0 ◯ Example 7-1 Compound 0.05 part by1³⁾ mass Comparative Comparative B Compound 2²⁾ B 3.0 7.2 X Example 7-2Compound 0.01 part by 2⁴⁾ mass Comparative Compound A — — 1.4 5.4 ◯Example 7-3 No. 4 0.02 part by mass Comparative — — Compound 1¹⁾ A 0.82.6 X Example 7-4 0.02 part by mass Comparative Compound B Compound 1¹⁾B 2.7 6.7 X Example 7-5 No. 4 0.01 part by 0.01 part by mass massComparative Compound B Compound 1¹⁾ A 1.7 5.2 X Example 7-6 No. 4 0.01part by 0.01 part by mass mass Comparative Compound A Compound 1¹⁾ B 1.95.6 Δ Example 7-7 No. 4 0.01 part by 0.01 part by mass mass ¹⁾Compound1: tris(2,4-di-tert-butylphenyl)phosphite ²⁾Compound 2:2,2′-methylenebis(4,6-di-tert-butylphenyl)-octadecyl phosphite³⁾Comparative Compound 1:tetrakis[3-(3,5-di-tert-butyl-4-hydroxyphenyl)propionyloxymethyl]methane⁴⁾Comparative Compound 2:1,3,5-tris(3-hydroxy-4-tert-butyl-2,6-dimethylbenzyl)isocyanurate ⁵⁾Method of addition A: A stabilizer was added upon polymerization ofolefin monomers, and calcium stearate was then added, followed bygranulation with an extruder at an extrusion temperature of 230° C. B:After polymerization of olefin monomers, a stabilizer and calciumstearate were added to the resulting polymer, followed by mixing of theresulting mixture and granulation using an extruder at an extrusiontemperature of 230° C. ⁶⁾ Stability: After leaving the fiber to stand at120° C. in an oven for 15 hours, the fiber was subjected to a tensiletest.

In Comparative Examples 7-1 and 7-2 and Comparative Examples 7-5 to 7-7,wherein a stabilizer(s) was/were added after polymerization of olefinmonomers and granulation was then performed, the initial yellownessindex (Y. I.) was high. Increase in yellowness was especially large inComparative Example 7-1 compared to the fibers of the present inventionin Examples 7-1 and 7-2 in spite of the fact that a 5 times largeramount of a commonly used stabilizer was blended in Comparative Example7-1. Thus, the fiber in Comparative Example 7-1 was more likely to beaffected by a NOx gas, and the effect of addition of the stabilizers waspoor in this fiber.

Further, although other types of a phenolic antioxidant and aphosphorus-containing antioxidant were used in Comparative Example 7-2,the stabilization effect was poor again in this fiber compared to thefibers of the present invention.

Further, in Comparative Examples 7-3 and 7-4, certain degrees of theeffect of suppression of the initial yellowness were observed in thecases where a phenolic antioxidant or a phosphorus-containingantioxidant was added alone upon polymerization of olefin monomers.However, in the case of Comparative Example 7-3, wherein a phenolicantioxidant was added alone, the fiber was likely to be affected by aNOx gas, and, in the case of Comparative Example 7-4, wherein aphosphorus-containing antioxidant was added alone, the obtained fiberitself lacked stability and the fiber was likely to be broken althoughthe fiber was not likely to be affected by a NOx gas.

In contrast, as is evident from Examples 7-1 and 7-2, the olefin powdersof the present invention were not likely to be affected by a NOx gas,and the obtained fibers had excellent stability.

From the above results, it could be confirmed that, by adding acombination of a specific phenolic antioxidant, which was masked by anorganoaluminum compound, and a phosphorus-containing antioxidant beforeor during polymerization of olefin monomers, the influence of a NOx gascan be suppressed and a fiber showing lower yellowness can be obtained.

1. A method for producing a stabilized olefin polymer, wherein anadditive(s) and a promoter component(s) are supplied to olefin monomersupon polymerization of said olefin monomers, wherein said methodcomprises a step wherein a slurry additive(s) is/are pumped while beingmixed with a promoter component(s) in a pipe(s), followed bytransferring the resulting mixture to a polymerization tank for olefinmonomers.
 2. The method for producing a stabilized olefin polymeraccording to claim 1, wherein said promoter component(s) is/are anorganoaluminum compound(s).
 3. The method for producing a stabilizedolefin polymer according to claim 1, wherein said promoter component(s)is/are a trialkyl aluminum(s).
 4. The method for producing a stabilizedolefin polymer according to claim 1, wherein said additive(s)comprise(s) a phenolic antioxidant represented by the General Formula(1) below:

(wherein R represents C₁₂-C₂₄ alkyl which is optionally branched, C₃-C₁₂cycloalkyl which is optionally substituted, or C₆-C₁₈ aryl whichoptionally has a substituent(s)) and is/are prepared by dissolving aliquid phenolic antioxidant(s) and/or a powdered phenolic antioxidant(s)in a solvent or by mixing a powdered phenolic additive(s) in an inertsolvent.
 5. The method for producing a stabilized olefin polymeraccording to claim 1, wherein said additive(s) preliminarily dissolvedin a solvent is/are supplied to said pipe(s) for transferring saidpromoter component(s) to said polymerization tank for olefin monomers,to mix said promoter component(s) with said additive(s) in said pipe(s).6. The method for producing a stabilized olefin polymer according toclaim 1, wherein said solvent is selected from aliphatic hydrocarbonsand alicyclic hydrocarbons.
 7. The method for producing a stabilizedolefin polymer according to claim 1, wherein said pipe(s) is/are apipe(s) having a line mixer.
 8. The method for producing a stabilizedolefin polymer according to claim 1, wherein the concentration of saidadditive component(s) is within the range of 1 to 80% by mass in saidslurry additive(s).